KR102376273B1 - Fuel Gas Supply System and Method for a Ship - Google Patents

Abstract

The present invention relates to a fuel supply system and method for a ship that supplies gas fuel to an engine, and to a fuel supply system and method for a ship capable of reducing the amount of air pollutants in exhaust gas, such as nitrogen oxide.
A fuel supply system for a ship according to the present invention, an engine for mixing liquefied gas and hydrogen gas; a mixing vessel for generating fuel gas by mixing vaporized liquefied gas and vaporized hydrogen gas; a fuel gas compressor for compressing the fuel gas supplied to the engine to a pressure required by the engine; and a compressed hydrogen tank for compressing and storing the surplus evaporated hydrogen gas in the fuel gas compressor, including, supplying the fuel gas generated in the mixing container as the fuel of the engine, and supplying the fuel gas of the engine and remaining evaporated Hydrogen gas is characterized in that it is stored in the compressed hydrogen tank.

Description

Fuel Gas Supply System and Method for a Ship

The present invention relates to a fuel supply system and method for a ship that supplies gas fuel to an engine, and to a fuel supply system and method for a ship capable of reducing the amount of air pollutants in exhaust gas, such as nitrogen oxide.

Worldwide, regulations on ship emissions and greenhouse gases are being strengthened. For example, according to the recent Air Pollution Control Agreement of the Marine Environment Protection Committee (MEPC) under the International Maritime Organization (IMO), the amount of nitrogen oxides (NO _x ) in exhaust gas is about 14.4 g/ Tier II, which regulates to satisfy kWh, came into effect in 2011, and Tier III, which was more strictly enforced, was applied restrictively from January 1, 2016.

In other words, ships built after 2016 and operating in the ECA (Emission Control Area) area of the United States including North America and the Caribbean must satisfy Tier III regulations and reduce NOx emissions from _14.4g /kWh to 3.4g/ should be reduced to kWh. In addition, the designation of ECA regions will continue to expand in the future, and the regulatory value is also expected to be strengthened.

As a method to satisfy the nitrogen oxide emission regulations of ships, typically, a Selective Catalytic Reduction (SCR) system is installed to supply urea water to the exhaust gas discharged from the engine to reduce nitrogen oxides to nitrogen (N ₂ ) and water (H ₂ O), or by installing an EGR (Exhaust Gas Recirculation) system to cool and purify part of the exhaust gas discharged from the engine, mix it with combustion air, and supply it back to the engine for combustion. There is a method to suppress the formation of nitrogen oxides.

On the other hand, even if such a clean technology is applied, it is known that the effect is lower than that of using natural gas (NG), which is a clean fuel, as a fuel. When natural gas is used as a ship's propulsion fuel, compared to using diesel fuel such as HFO (Heavy Fuel Oil), there is almost no emission of fine dust and sulfur oxides (SO _x ), and greenhouse gases such as nitrogen oxides and carbon dioxide emissions can be significantly reduced.

Nitrogen oxide (NO _x ) is mainly generated by a chemical reaction of nitrogen (N ₂ ) and oxygen (O ₂ ) in the combustion process under high temperature and high pressure in the combustion chamber of the engine. The EGR system is a method of reducing the amount of nitrogen oxides produced by supplying only as much oxygen as necessary for combustion of fuel into the combustion chamber of the engine in order to suppress the production of nitrogen oxides, thereby minimizing the amount of oxygen used to generate nitrogen oxides. After combustion, exhaust gas containing a large amount of carbon dioxide is cooled and cleaned, mixed with combustion air, and supplied to the engine to increase the carbon dioxide concentration in the combustion air and lower the oxygen concentration to reduce the generation of nitrogen oxides. is to suppress

As described above, in the EGR system that recirculates a part of exhaust gas to the combustion air of the engine, the initial investment cost is high because there are many additional equipment added to the engine. The disadvantage is that it is higher than this existing engine. In addition, there is a problem in that a neutralizer (NaOH) supply is required while the EGR system is operating, and residual substances such as sludge are generated and must be treated.

On the other hand, similarly when natural gas is used as an engine fuel, nitrogen oxides are generated in large amounts, and additional equipment must be installed to satisfy emission regulations. Accordingly, there is a demand for a method capable of reducing the emission of nitrogen oxides even in ships using LNG as an engine fuel.

Accordingly, an object of the present invention is to solve the above problems, and to provide a fuel supply system and method for a ship capable of reducing the amount of air pollutants such as nitrogen oxide and carbon dioxide in exhaust gas of a marine engine .

According to an aspect of the present invention for achieving the above object, an engine for mixing liquefied gas and hydrogen gas; a mixing vessel for generating fuel gas by mixing vaporized liquefied gas and vaporized hydrogen gas; a fuel gas compressor for compressing the fuel gas supplied to the engine to a pressure required by the engine; and a compressed hydrogen tank that compresses and stores the surplus evaporated hydrogen gas in the fuel gas compressor. A fuel supply system for a ship is provided, wherein hydrogen gas is stored in the compressed hydrogen tank.

Preferably, a hydrogen storage line connecting the compressed hydrogen tank and the engine, and mixing the compressed hydrogen gas stored in the compressed hydrogen tank with the fuel gas supplied to the engine; may further include.

Preferably, the engine comprises: a low-pressure gas engine using a low-pressure fuel gas as a fuel; and a high-pressure gas engine using high-pressure fuel gas as a fuel, wherein the fuel gas compressor may compress fuel gas to a pressure required by the high-pressure gas engine.

Preferably, a heat exchanger for cooling the vaporized liquefied gas by exchanging the vaporized liquefied gas and the vaporized hydrogen gas; and a gas-liquid separator for gas-liquid separation between the evaporative liquefied gas reliquefied by the cooling and heat of the evaporative hydrogen gas in the heat exchanger and the evaporative liquefied gas that is not reliquefied in the heat exchanger. The gas is supplied to the mixing vessel, and the reliquefied vaporized liquefied gas in the liquid state separated in the gas-liquid separator may be recovered to the liquefied gas storage tank.

Preferably, a hydrogen gas flow valve for controlling the flow rate of the evaporated hydrogen gas supplied to the heat exchanger; a liquefied gas flow valve for controlling the flow rate of evaporative liquefied gas supplied to the heat exchanger; and a control unit controlling a mixing ratio of the fuel gas mixed in the mixing vessel by controlling the hydrogen gas flow valve and the liquefied gas flow valve.

Preferably, a hydrogen gas compressor for compressing the evaporated hydrogen gas supplied to the heat exchanger to a pressure required by the low-pressure gas engine; and a liquefied gas compressor for compressing the evaporative liquefied gas supplied to the heat exchanger to a pressure required by the low-pressure gas engine; Low-pressure evaporation liquefied gas may be supplied to the heat exchanger.

Preferably, a second recovery line for recovering the condensate condensed in the mixing vessel to the liquefied gas storage tank; may further include.

Preferably, a fuel control line for re-supplying some of the fuel gas compressed in the fuel gas compressor to the mixing vessel; and a control unit controlling the on/off valve of the fuel control line to adjust the mixing ratio of the fuel gas mixed in the mixing vessel, wherein the control unit opens the fuel control line to remove the condensate in the mixing vessel. can be vaporized.

According to another aspect of the present invention for achieving the above object, in the fuel supply method of a ship including a liquid hydrogen storage tank and a liquid hydrogen storage tank, the vaporized liquefied gas and liquid hydrogen generated in the liquid hydrogen storage tank Each of the evaporative hydrogen gas generated in the storage tank is compressed, the evaporative liquefied gas and the evaporative hydrogen gas are heat-exchanged in a heat exchanger to cool the evaporative liquefied gas, and cooled by the heat exchange with the evaporative hydrogen gas whose temperature is increased by the heat exchange. A fuel gas mixed with the evaporated liquefied gas is supplied as a fuel for the engine, and the remaining evaporated hydrogen gas is further compressed and stored in a compressed hydrogen tank after being supplied as the fuel, a fuel supply method for ships is provided.

Preferably, the evaporative liquefied gas reliquefied by the heat exchange is recovered to a liquefied gas storage tank, and the vaporized liquefied gas in a gaseous state not reliquefied by the heat exchange is mixed with the evaporative hydrogen gas as fuel of the engine. can supply

Preferably, the mixing ratio of the fuel gas may be adjusted by controlling the flow rates of the vaporized liquefied gas supplied to the heat exchanger and the vaporized hydrogen gas supplied to the heat exchanger.

Preferably, the fuel gas may be supplied to a fuel gas compressor, compressed to a high pressure required by the high-pressure gas engine, and the compressed fuel gas may be supplied to the high-pressure gas engine.

Preferably, the evaporative liquefied gas and the evaporative hydrogen gas supplied to the heat exchanger are compressed to a low pressure required by the low-pressure gas engine, respectively, and the fuel gas obtained by mixing the evaporative liquefied gas and the evaporative hydrogen gas compressed to the low pressure after heat exchange is used as the fuel gas. It can be supplied by a low-pressure gas engine.

Preferably, when the high-pressure gas engine is not operated and only the low-pressure gas engine is operated, the fuel gas is supplied as fuel of the low-pressure gas engine, and the surplus evaporated hydrogen gas is compressed and stored in the fuel gas compressor. can

Preferably, when the evaporative hydrogen gas generated from the liquid hydrogen storage tank is insufficient, the stored evaporative hydrogen gas and the evaporative liquefied gas may be mixed and supplied as a fuel of the high-pressure gas engine.

The fuel supply system and method for a ship according to the present invention can use natural gas as a fuel for a marine engine, and in particular, by using a fuel gas obtained by mixing natural gas with hydrogen gas in a certain ratio, nitrogen oxides in exhaust gas and The amount of carbon dioxide can be reduced.

In addition, by controlling the mixing ratio of natural gas and hydrogen gas and uniformly mixing natural gas and hydrogen, combustion safety of the engine can be improved.

In addition, since the evaporative natural gas can be recovered by re-liquefaction, it can be used without wasting the evaporative natural gas, which is economical and eco-friendly.

In addition, since the evaporative natural gas is reliquefied using the cooling heat of evaporative hydrogen gas, the energy required to liquefy the evaporative natural gas can be minimized.

In addition, when a large amount of evaporative hydrogen gas is generated, by storing the surplus evaporative hydrogen gas, all of the evaporative hydrogen gas can be used without wasting, and when necessary, it can be reused as an engine fuel, which is economical and eco-friendly.

1 is a configuration diagram schematically illustrating a fuel supply system according to a first embodiment of the present invention.
2 is a configuration diagram schematically illustrating a fuel supply system according to a second embodiment of the present invention.
3 is a block diagram schematically illustrating a fuel supply system according to a third embodiment of the present invention.
4 is a diagram illustrating a fluid flow diagram according to a first operation mode using the fuel supply system according to the third embodiment of the present invention shown in FIG. 3 .
FIG. 5 is a diagram illustrating a fluid flow diagram according to a second operation mode using the fuel supply system according to the third embodiment of the present invention shown in FIG. 3 .
6 is a diagram illustrating a fluid flow diagram according to a third operation mode using the fuel supply system according to the third embodiment of the present invention shown in FIG. 3 .

In order to fully understand the operational advantages of the present invention and the objects achieved by the practice of the present invention, reference should be made to the accompanying drawings illustrating preferred embodiments of the present invention and the contents described in the accompanying drawings.

Hereinafter, the configuration and operation of the preferred embodiment of the present invention will be described in detail with reference to the accompanying drawings. Here, it should be noted that in adding reference signs to the elements of each drawing, the same elements are indicated with the same reference numerals as much as possible even though they are indicated on different drawings.

A fuel supply system according to embodiments of the present invention, which will be described later, will be described with reference to an example applied to a marine engine. However, the present invention is not limited thereto, and the fuel supply system according to embodiments of the present invention may be applied to a land engine.

In one embodiment of the present invention, the vessel may be any type of vessel in which an engine capable of using liquefied gas as a fuel for a propulsion engine or a fuel for a power generation engine is installed. In addition, any type of vessel using liquefied gas as a fuel may be applied to the vessel according to an embodiment of the present invention. For example, including ships with self-propelled capabilities such as LNG carriers, liquid hydrogen carriers, and LNG RVs (Regasification Vessels), LNG Floating Production Storage Offloading (FPSO), LNG FSRU (Floating Storage Regasification Unit) and May include offshore structures that do not have the same propulsion capability but are floating in the sea. However, in the embodiment to be described later, a liquefied gas carrier or a liquid hydrogen carrier will be described as an example.

In addition, in embodiments of the present invention, the engine may be an engine capable of mixing liquefied gas and hydrogen gas.

In addition, the liquefied gas may be a liquefied gas that can be transported by liquefying the gas at a low temperature, for example, LNG (Liquefied Natural Gas), LEG (Liquefied Ethane Gas), LPG (Liquefied Petroleum Gas), liquefied ethylene gas It may be a liquefied petrochemical gas, such as (Liquefied Ethylene Gas) or liquefied propylene gas (Liquefied Propylene Gas). However, in the embodiments to be described later, an example in which LNG, which is a representative liquefied gas, is applied will be described.

That is, in the embodiments of the present invention to be described later, the liquefied gas fuel will be described as an example of LNG.

1 to 3 are schematic diagrams illustrating a fuel supply system according to an embodiment of the present invention, and FIGS. 4 to 6 are fuel supply systems according to an operation mode of the fuel supply system according to an embodiment of the present invention. It is a diagram showing a flowchart of Hereinafter, a fuel supply system and method for a ship according to an embodiment of the present invention will be described with reference to FIGS. 1 to 6 .

First, a fuel supply system according to a first embodiment of the present invention will be described with reference to FIG. 1 .

A fuel supply system according to a first embodiment of the present invention, as shown in Figure 1, an LNG storage tank 100 for storing LNG; Liquid hydrogen storage tank 200 for storing liquid hydrogen (Liquid Hydrogen, LH ₂ ); A mixing vessel 300 for uniformly mixing the evaporative natural gas generated by natural vaporization of the LNG stored in the LNG storage tank 100 and the evaporative hydrogen gas generated by the natural vaporization of the liquid hydrogen stored in the liquid hydrogen storage tank 200; a fuel gas compressor 310 for compressing the fuel mixed in the mixing vessel 300 to the pressure required by the engine 400; and a high-pressure gas engine 400 that uses natural gas as a fuel and can mix natural gas and hydrogen gas.

1, the LNG storage tank 100 and the liquid hydrogen storage tank 200 are respectively provided one by one as an example, but the LNG storage tank 100 and the liquid hydrogen storage tank 200 of this embodiment are each at least one. may be provided separately.

In addition, in FIG. 1 , the LNG storage tank 100 and the liquid hydrogen storage tank 200 are provided as an example having the same shape and the same size (capacity), but the LNG storage tank 100 and the liquid of this embodiment The hydrogen storage tank 200 may be provided with different shapes and different sizes (capacities).

The LNG storage tank 100 of this embodiment is preferably insulated so that the LNG can be stored while maintaining the liquid state while the ship is operating. In this embodiment, LNG may be stored in the LNG storage tank 100 at about 1.1 bar to about -163°C.

In addition, the LNG storage tank 100 of the present embodiment may be a cargo storage tank for storing LNG as cargo to transport it, or may be separately provided for fuel storage of an engine.

In addition, the LNG storage tank 100 may be manufactured to withstand the pressure rise due to boil-off gas generated by natural vaporization due to external heat intrusion in the LNG storage tank 100 up to a set pressure, When the internal pressure exceeds the set pressure, the safety valve may be opened to discharge the boil-off gas in the storage tank. In this embodiment, the evaporative natural gas discharged from the LNG storage tank 100 flows along the evaporative natural gas line NL and is supplied as fuel of the engine or is recovered to the LNG storage tank 100 in a liquid state.

The liquid hydrogen storage tank 200 of this embodiment may be insulated so that liquid hydrogen can be stored while maintaining a liquid state while the ship is operating. In addition, the liquid hydrogen storage tank 200 may be a high-pressure pressure vessel for storing hydrogen at a high pressure.

In addition, the liquid hydrogen storage tank 200 may be manufactured to withstand the pressure rise due to the boil-off gas generated by natural vaporization by external heat intrusion in the liquid hydrogen storage tank 200 up to a set pressure, and storage When the internal pressure of the tank exceeds the set pressure, the safety valve may be opened to discharge the boil-off gas in the storage tank. In this embodiment, the evaporated hydrogen gas discharged from the liquid hydrogen storage tank 200 flows along the evaporated hydrogen gas line HL and may be supplied as fuel of the engine.

The mixing vessel 300 of this embodiment accommodates the evaporated natural gas discharged from the LNG storage tank 100 and the evaporated hydrogen gas discharged from the liquid hydrogen storage tank 200, and a pressure vessel for uniformly mixing the two gases. ) can be The mixing vessel 300 may supply a gaseous fuel gas obtained by uniformly mixing the evaporated natural gas and the evaporated hydrogen gas as the fuel of the engine 400 .

In addition, the mixing vessel 300 is connected from the LNG storage tank 100, the evaporative natural gas line (NL) through which the evaporative natural gas flows from the LNG storage tank 100 to the mixing vessel 300; and an evaporated hydrogen gas line (HL) connected from the liquid hydrogen storage tank 200 and through which the evaporated hydrogen gas flows from the liquid hydrogen storage tank 200 to the mixing vessel 300; is connected.

In the evaporative natural gas line (NL), the natural gas flow valve 120 for controlling the flow rate of the evaporative natural gas supplied from the LNG storage tank 100 to the mixing vessel 300; and a natural gas flow rate transmitter 121 for measuring the flow rate of evaporated natural gas supplied to the mixing vessel 300 .

In the evaporated hydrogen gas line (HL), a hydrogen gas flow valve 220 for controlling the flow rate of the evaporated hydrogen gas supplied from the liquid hydrogen storage tank 200 to the mixing vessel 300; and a hydrogen gas flow rate transmitter 221 for measuring the flow rate of evaporated hydrogen gas supplied to the mixing vessel 300 .

In the control unit (not shown), the flow rate of the evaporative natural gas supplied from the natural gas flow transmitter 121 to the mixing vessel 300 is measured, and the opening and closing of the natural gas flow valve 120 is adjusted according to the measured value, whereby the mixing vessel It is possible to control the flow rate of the evaporative natural gas supplied to (300).

In addition, the control unit measures the flow rate of evaporated hydrogen gas supplied from the hydrogen gas flow transmitter 221 to the mixing vessel 300, and adjusts the opening and closing of the hydrogen gas flow valve 220 according to the measured value, thereby increasing the mixing vessel ( 300) can control the flow rate of the evaporated hydrogen gas supplied to.

Therefore, according to the present embodiment, it is possible to control the flow rate of the evaporative natural gas and the evaporative hydrogen gas supplied to the mixing vessel 300 to adjust the natural gas and hydrogen mixing ratio of the fuel gas to be supplied as the fuel of the engine 400 .

For example, the engine 400 of this embodiment is capable of co-firing natural gas and hydrogen gas, and when burning fuel gas in which natural gas and hydrogen gas are mixed in an appropriate ratio, compared to burning only natural gas, nitrogen oxide ( NO _x ), the amount of carbon dioxide (CO ₂ ) generated is reduced. However, if the mixing ratio of the hydrogen gas in the fuel gas is too high, incomplete combustion may occur and instead, environmental pollutants such as carbon monoxide (CO) may be discharged. Accordingly, the control unit may adjust the mixing ratio of the fuel gas mixed in the mixing vessel 300 by adjusting the flow rates of the natural gas and hydrogen gas supplied to the mixing vessel 300 .

The mixing ratio of the fuel gas mixed in the mixing vessel 300 may be a preset value or may be changed in real time according to the load of the engine 400 .

In addition, the mixing vessel 300 of this embodiment is connected to the engine 400 and the fuel gas mixed in the mixing vessel 300 flows from the mixing vessel 300 to the engine 400 high-pressure fuel gas line (FL1) ; and a second recovery line RL2 through which the condensate (drain) condensed in the mixing vessel 300 is discharged from the mixing vessel 300 and flows; is connected.

A flow rate of fuel gas supplied from the mixing vessel 300 to the engine 400 along the high-pressure fuel gas line FL1 may be adjusted according to the amount of fuel gas required by the engine 400 .

Some of the fuel gas discharged from the mixing vessel 300 and compressed in the fuel gas compressor 310 is fuel controlled to control the water level in the mixing vessel 300 or to control the mixing ratio of natural gas and hydrogen gas It may be re-supplied to the mixing vessel 300 along the line PL1.

For example, the control unit opens the fuel control line PL1 to re-supply some of the fuel gas compressed in the fuel gas compressor 310 to the mixing container 300 , so that by compression in the fuel gas compressor 310 . The condensate in the mixing vessel 300 may be vaporized by the fuel gas whose temperature has risen.

Since the boiling point of hydrogen is lower than the boiling point of natural gas (methane) under the same pressure condition, the temperature of the evaporated hydrogen gas supplied to the mixing vessel 300 may be lower than the temperature of the evaporated natural gas. Therefore, in the mixing vessel 300, a portion of the evaporated natural gas may be condensed by the cooling and heat of the evaporated hydrogen gas. The evaporated natural gas condensed in the mixing vessel 300 may be discharged from the mixing vessel 300 along the second recovery line RL2 .

The second recovery line RL2 of this embodiment may be connected from the mixing vessel 300 to the LNG storage tank 100 . That is, the condensate discharged from the mixing vessel 300 may be condensed evaporative natural gas, and the condensed evaporative natural gas is recovered to the LNG storage tank 100 .

The second recovery line RL2 may include a valve whose opening and closing is controlled by the controller, and the opening and closing of the second recovery line RL2 may be controlled according to a liquid level in the mixing vessel 300 . there is. That is, when the water level in the mixing vessel 300 is higher than the set value, the control unit may open the valve so that the condensed BOG is discharged from the mixing vessel 300 .

In the high-pressure fuel gas line FL1 of this embodiment, a fuel gas compressor 310 for compressing the fuel gas supplied to the engine 400 from the mixing vessel 300 to the pressure required by the engine 400; is provided.

The engine 400 of this embodiment may mix natural gas and hydrogen gas, and may be a high-pressure gas engine 400 . The high-pressure gas engine 400 may be, for example, a ME-GI engine (MAN Electronic Gas Injection Engine). The ME-GI engine is composed of two strokes, and is a high-pressure gas injection engine employing a diesel cycle in which high-pressure natural gas of about 300 bar is directly injected into the combustion chamber near the top dead center of the piston. The ME-GI engine requires a high-pressure fuel gas supply pressure of about 200 to 400 bara (absolute pressure) depending on the load. The ME-GI engine may be provided as an engine for propulsion of a ship.

Accordingly, the fuel gas compressor 310 of the present embodiment can compress the fuel gas supplied from the mixing vessel 300 to the high-pressure gas engine 400 to a high pressure required by the high-pressure gas engine 400 . In this embodiment, the fuel gas compressor 310 may compress the fuel gas to about 100 bar to 400 bar, or about 150 bar to 300 bar.

In this embodiment, by relatively reducing the concentration of natural gas reacting with oxygen in the combustion chamber by hydrogen supplied together with natural gas to the combustion chamber of the high-pressure gas engine 400, the specific heat inside the combustion chamber is increased and combustion energy By absorbing , the peak temperature inside the combustion chamber, that is, the combustion temperature, is lowered, and thus the chemical reaction generating nitrogen oxide can be weakened.

In addition, according to the present embodiment, the fuel control line PL1 branched from the high-pressure fuel gas line FL1 and re-supplying a part of the fuel gas compressed in the fuel gas compressor 310 to the mixing vessel 300; provided

The amount of fuel gas branched to the fuel control line PL1 may be adjusted by a control unit that controls a valve provided in the fuel control line PL1. The controller may adjust the flow rate of the fuel gas supplied to the high-pressure gas engine 400 by controlling the valve of the fuel control line PL1 .

For example, if the flow rate of fuel gas compressed by the fuel gas compressor 310 and supplied to the high-pressure gas engine 400 is greater than the amount required by the high-pressure gas engine 400 , the control unit may By opening the valve and adjusting the opening amount, a portion of the fuel gas compressed by the fuel gas compressor 310 and supplied to the high-pressure gas engine 400 may be re-supplied to the mixing vessel 300 . Alternatively, the valve of the fuel control line PL1 may be opened when fuel cannot be used, such as when the high-pressure gas engine 400 is shut down.

In addition, the controller may control the valve of the fuel control line PL1 to vaporize the condensed evaporative natural gas as described above, and to adjust the flow rate of the fuel gas re-supplied to the mixing vessel 300 . The control unit controls the valve of the fuel control line PL1 to re-supply some of the fuel gas compressed in the fuel gas compressor 310 to the mixing vessel 300, and in the mixing vessel 300, the fuel gas compressor ( 310), the condensed evaporative natural gas is vaporized by the fuel gas whose temperature has risen while being compressed.

For example, when it is desired to supply a larger amount of fuel gas from the mixing vessel 300 , or from the mixing vessel 300 along the high-pressure fuel gas line FL1 , the fuel of the high-pressure gas engine 400 is supplied. When it is desired to increase the ratio of natural gas in fuel gas, by opening the fuel control line PL1 and supplying some of the fuel gas compressed in the fuel gas compressor 310 to the mixing vessel 300 to vaporize the condensed evaporative natural gas. , it is possible to increase the proportion of natural gas in the fuel gas discharged from the mixing vessel 300 through the high-pressure fuel gas line FL1.

According to this embodiment, the natural gas compressor 110 is provided in the evaporative natural gas line (NL) for compressing the evaporative natural gas supplied from the LNG storage tank 100 to the mixing vessel 300 to a low pressure; and a hydrogen gas compressor 210 provided in the evaporated hydrogen gas line HL and compressed to a low pressure for the evaporated hydrogen gas supplied from the liquid hydrogen storage tank 200 to the mixing vessel 300 .

In addition, according to the present embodiment, the heat exchanger 130 for heat exchange between the evaporative natural gas compressed to a low pressure in the natural gas compressor 110 and the evaporative hydrogen gas compressed to a low pressure in the hydrogen gas compressor 210; do.

In the heat exchanger 130 of this embodiment, the evaporative natural gas compressed to a low pressure and evaporative hydrogen gas compressed to a low pressure exchange heat, and the evaporative natural gas compressed to a low pressure is cooled by the cooling heat of the evaporative hydrogen gas compressed to a low pressure. and is supplied to the mixing vessel 300 . In addition, while cooling the evaporated natural gas compressed to a low pressure in the heat exchanger 130 , the low-pressure compressed hydrogen gas having an increased temperature is supplied to the mixing vessel 300 .

The temperature of the evaporated natural gas and the evaporated hydrogen gas discharged after heat exchange in the heat exchanger 130 may be adjusted by controlling the natural gas flow valve 120 and the hydrogen gas flow valve 220 described above by the controller.

For example, when it is desired to lower the cooling temperature of the low-pressure evaporative natural gas discharged from the heat exchanger 130 , the hydrogen gas flow valve 220 is controlled to allow a greater amount of hydrogen gas to flow into the heat exchanger 130 . supply can be adjusted.

Alternatively, when the amount of evaporative natural gas supplied to the heat exchanger 130 increases, the controller controls the hydrogen gas flow valve 220 so that a larger amount of hydrogen gas is supplied to the heat exchanger 130 and heat exchanges. The temperature of the evaporated natural gas supplied to the mixing vessel 300 through the unit 130 may be constantly maintained.

The above-described hydrogen gas flow valve 220 may be provided at the front end of the heat exchanger 130 , and the hydrogen gas flow rate transmitter 221 may be provided at the rear end of the heat exchanger 130 and at the front end of the mixing vessel 300 .

In addition, the above-described natural gas flow valve 120 is provided at the front end of the heat exchanger 130 , and the natural gas flow transmitter 121 is provided at the rear end of the heat exchanger 130 and at the front end of the mixing vessel 300 . there is. More specifically, the natural gas flow rate transmitter 121 may be provided at the rear end of the gas-liquid separator 140 to be described later, and at the front end of the mixing vessel 300 .

The vaporized natural gas line NL of this embodiment may further include a gas-liquid separator 140 for gas-liquid separation of the vaporized natural gas supplied to the mixing vessel 300 .

The vaporized natural gas in the gaseous state separated by the gas-liquid separator 140 of this embodiment is supplied to the mixing vessel 300 . In addition, the vaporized natural gas in the liquid state separated in the gas-liquid separator 140 is to be recovered to the LNG storage tank 100 along the first recovery line RL connected from the gas-liquid separator 140 to the LNG storage tank 100 . can

The evaporative natural gas discharged from the LNG storage tank 100 is compressed to a low pressure in the natural gas compressor 110 , and is cooled by heat exchange with the low-pressure evaporative hydrogen gas in the heat exchanger 130 . The low-pressure evaporative natural gas may be partially reliquefied while being cooled by heat exchange with the low-pressure evaporative hydrogen gas in the heat exchanger 130 . Accordingly, the gas-liquid separator 140 may be supplied with a gas-liquid mixture of low-pressure evaporative natural gas, and the evaporative natural gas reliquefied by the cooling and heat of the low-pressure evaporative hydrogen gas is transferred to the LNG storage tank 100 along the first recovery line RL1. ) is returned.

The controller may control the opening and closing of the valve of the first recovery line RL1 so that the reliquefied evaporative natural gas is recovered from the gas-liquid separator 140 to the LNG storage tank 100 . For example, when the water level of the gas-liquid separator 140 reaches the set value or more, the control unit opens the valve of the first recovery line RL1 to recover the reliquefied evaporated natural gas to the LNG storage tank 100 . can make it happen

In addition, when the amount of evaporative natural gas is greater than the amount required by the engine 400 , the control unit controls so that a larger amount of evaporative natural gas is reliquefied from the gas-liquid separator 140 to the LNG storage tank 100 . It can also be controlled to increase the amount of reliquefied BOG recovered to the furnace.

According to this embodiment, a portion of the low-pressure evaporative natural gas that is branched from the evaporative natural gas line (NL) at the rear end of the natural gas compressor 110 and supplied to the heat exchanger 130 bypasses the heat exchanger 130 and the heat exchanger (130) The first evaporative natural gas branch line NL1 to be introduced into the downstream flow; may be further provided.

The controller may control the valve of the first evaporative natural gas branch line NL1 to adjust the flow rate of the low-pressure evaporative natural gas that is not supplied to the heat exchanger 130 in the low-pressure evaporative natural gas.

For example, when the temperature of the evaporative natural gas at the rear end of the heat exchanger 130 is lower than the set value, the control unit opens the valve of the first evaporative natural gas branch line NL1 so that the evaporative natural gas is transferred to the heat exchanger 130 . By allowing the heat exchanger 130 to join the downstream flow without heat exchange in the heat exchanger 130, the temperature of the natural gas vaporized at the rear end of the heat exchanger 130 can be increased.

In addition, the control unit may control the valve of the first evaporative natural gas branch line NL1 to adjust the amount of evaporative natural gas reliquefied by heat exchange, and is supplied from the gas-liquid separator 140 to the mixing vessel 300 . It is also possible to adjust the flow rate of the evaporated natural gas.

For example, when it is desired to supply a larger amount of evaporative natural gas from the gas-liquid separator 140 to the mixing vessel 300 , the control unit opens the valve of the first evaporative natural gas branch line NL1 to increase the amount By allowing the evaporated natural gas of the to be supplied to the gas-liquid separator 140 without being cooled in the heat exchanger 130, the reliquefied evaporative natural gas existing in the liquid state in the gas-liquid separator 140 is vaporized to vaporize the gaseous state Natural gas may be supplied to the mixing vessel 300 .

Hereinafter, with reference to FIG. 1, a method of supplying fuel gas obtained by mixing natural gas and hydrogen gas at an appropriate mixing ratio to a high-pressure gas engine 400 for a ship using a fuel supply system for a ship according to an embodiment of the present invention to explain

The evaporative natural gas from the LNG storage tank 100 is discharged along the evaporative natural gas line NL, and compressed at a low pressure in the natural gas compressor 110 . In addition, the evaporated hydrogen gas from the liquid hydrogen storage tank 200 is discharged along the evaporated hydrogen gas line HL, and compressed at a low pressure in the hydrogen gas compressor 210 .

The low-pressure evaporative natural gas compressed by the natural gas compressor 110 and the low-pressure evaporative hydrogen gas compressed by the hydrogen gas compressor 210 are heat-exchanged in the heat exchanger 130 . In the heat exchanger 130, the low-pressure evaporative natural gas is cooled by heat exchange, and the temperature of the low-pressure evaporative hydrogen gas is increased.

The control unit, the flow rate of fuel gas required by the high-pressure gas engine 400, the mixing ratio of the fuel gas supplied to the high-pressure gas engine 400, the temperature of the evaporative natural gas or evaporative hydrogen gas at the rear end of the heat exchanger 130 or The amount of opening and closing of the hydrogen gas flow valve 220 and the natural gas flow valve 120 is controlled according to factors such as the flow rate and the flow rate of the evaporated natural gas to be reliquefied. By controlling the hydrogen gas flow valve 220 and the natural gas flow valve 120 , the flow rates of the low-pressure evaporative natural gas and the low-pressure evaporative hydrogen gas supplied to the heat exchanger 130 can be adjusted.

After heat exchange in the heat exchanger 130 , the evaporated hydrogen gas having an increased temperature is supplied to the mixing vessel 300 .

The low-pressure evaporative natural gas cooled by heat exchange in the heat exchanger 130 is supplied to the gas-liquid separator 140 to separate the reliquefied evaporative natural gas from the non-reliquefied evaporative natural gas. The reliquefied evaporated natural gas separated in the gas-liquid separator 140 is recovered to the LNG storage tank 100 , and the evaporated natural gas that has not been reliquefied is supplied to the mixing vessel 300 .

In the mixing container 300 , the evaporated natural gas and the evaporated hydrogen gas supplied to the mixing container 300 are uniformly mixed. At this time, the control unit maintains a constant mixing ratio of the evaporative natural gas and the evaporative hydrogen gas by adjusting the flow rates of the evaporative natural gas and the evaporative hydrogen gas supplied to the mixing vessel 300, or may adjust the mixing ratio as necessary. .

In the mixing vessel 300 , the fuel gas in which the evaporative natural gas and the evaporative hydrogen gas are uniformly mixed according to the mixing ratio is discharged from the mixing vessel 300 along the high-pressure fuel gas line FL1 , and in the fuel gas compressor 310 . It is compressed to the pressure required by the high-pressure gas engine 400 , that is, high pressure, and supplied as fuel of the high-pressure gas engine 400 .

In the mixing vessel 300 , only gaseous fuel gas is supplied to the fuel gas compressor 310 , and the condensed and evaporated natural gas in the condensed liquid state is separately discharged and recovered to the LNG storage tank 100 .

The control unit controls a portion of the high-pressure fuel gas compressed in the fuel gas compressor 310 according to the flow rate of evaporative natural gas to be recovered to the LNG storage tank 100 and the amount or mixing ratio of fuel gas to be supplied to the high-pressure gas engine 400 . It can be controlled to re-supply to the mixing vessel (300).

By re-supplying the high-pressure fuel gas whose temperature has increased by compression in the fuel gas compressor 310 to the mixing vessel 300 , the condensed evaporative natural gas remaining in the liquid state in the mixing vessel 300 is vaporized, and high-pressure fuel The mixing ratio of the fuel gas supplied to the gas compressor 310 and the flow rate of the condensed evaporative natural gas recovered to the LNG storage tank 100 may be adjusted.

Next, a fuel supply system according to a second embodiment of the present invention will be described with reference to FIG. 2 .

The second embodiment of the present invention is a modified example of the first embodiment, and is different in that fuel is supplied to the low-pressure gas engine 500 . Hereinafter, the second embodiment of the present invention will be described focusing on the differences from the first embodiment. Even if the description is omitted, the same reference numerals may be applied in the same manner as in the first embodiment, and of course, may be modified within the design change range.

A fuel supply system according to a second embodiment of the present invention, as shown in Figure 2, an LNG storage tank (100); liquid hydrogen storage tank 200; and a mixing container 300 . The LNG storage tank 100 and the mixing vessel 300 are connected by an evaporative natural gas line (NL), and the liquid hydrogen storage tank 300 and the mixing vessel 300 are connected by an evaporative hydrogen gas line (HL). .

In addition, the fuel supply system according to this embodiment, using natural gas as a fuel, and a low-pressure gas engine 500 capable of mixing natural gas and hydrogen gas; includes.

The low-pressure gas engine 500 of this embodiment may be, for example, a DFDE engine (Dual Fuel Diesel Electric Engine). The DFDE engine consists of four strokes, and is a low-pressure gas injection engine employing an Otto Cycle in which a low-pressure natural gas of about 6.5 bar is injected into the combustion air inlet, and the piston rises and compresses it. The DFDE engine may be provided as an engine for power generation of a ship.

In addition, the evaporative natural gas line NL is provided with a natural gas compressor 110 for compressing the evaporative natural gas to a low pressure, and the evaporative hydrogen gas line HL is provided with a hydrogen gas compressor 210 for compressing the evaporative hydrogen gas to a low pressure. ); is provided.

The pressure for compressing natural gas in the natural gas compressor 110 of this embodiment and the pressure for compressing the hydrogen gas in the hydrogen gas compressor 210 may be the fuel gas pressure required by the low-pressure gas engine 400 of this embodiment. Alternatively, the pressure may be slightly higher than that in consideration of the pressure loss at the rear end.

That is, in the natural gas compressor 100 and the hydrogen gas compressor 210 of this embodiment, the pressure required by the low-pressure gas engine 500 for natural gas and hydrogen gas, respectively, is about 3 bar to 8 bar, or about 4 bar to 6.5 bar. compressed into bar.

In addition, according to the present embodiment, a heat exchanger 130 for cooling the low-pressure evaporative natural gas by heat-exchanging the low-pressure evaporative natural gas and the low-pressure evaporative hydrogen gas by cooling and heat of the low-pressure evaporative hydrogen gas; is provided.

The evaporative natural gas line (NL) includes a natural gas flow valve 120 for controlling the flow rate of the low-pressure evaporative natural gas introduced into the heat exchanger 130; and a natural gas flow rate transmitter 121 for measuring the flow rate of evaporated natural gas introduced into the mixing vessel 300 .

In addition, the hydrogen gas flow valve 220 for controlling the flow rate of the low-pressure evaporated hydrogen gas introduced into the heat exchanger 130 in the evaporated hydrogen gas line (HL); and a hydrogen gas flow rate transmitter 221 for measuring the flow rate of evaporated hydrogen gas introduced into the mixing vessel 300 .

A first evaporative natural gas branch line branching from the evaporative natural gas line NL and allowing the evaporative natural gas to bypass the heat exchanger 130 is further provided in the evaporative natural gas line NL.

In addition, the evaporative natural gas line (NL), the gas-liquid separator 140 for separating the evaporative natural gas reliquefied by the cooling heat of the evaporative hydrogen gas in the heat exchanger 130; is provided. The vaporized natural gas separated in the gas-liquid separator 140 is supplied to the mixing vessel 300 , and the separated liquid vaporized natural gas is recovered to the LNG storage tank 100 along the first recovery line RL1 . do.

In the mixing vessel 300, the evaporated hydrogen gas and the evaporated natural gas introduced into the mixing vessel 300 are uniformly mixed according to the mixing ratio. The fuel gas mixed in the mixing vessel 300 is supplied to the low pressure gas engine 500 along the low pressure fuel gas line FL2. In addition, the evaporated natural gas condensed in the mixing vessel 300 is recovered to the LNG storage tank 100 along the second recovery line RL2.

In addition, the low-pressure fuel gas line (FL2), a fuel control line (PL2) branched from the low-pressure fuel gas line (FL2) to re-supply a portion of the fuel gas to the mixing vessel 300; is further provided. The fuel control line PL2 is for adjusting the flow rate of the fuel gas supplied to the low-pressure gas engine 500 , adjusting the mixing ratio of the fuel gas mixed in the mixing vessel 300 , or for regulating the pressure in the mixing vessel 300 . can be used for this purpose. Alternatively, it may be utilized for the purpose of processing fuel gas in an emergency situation in which fuel gas cannot be supplied from the low-pressure gas engine 500 .

In addition, in the low-pressure fuel gas line FL2 , a fuel gas heater 320 that heats the temperature of the fuel gas supplied from the mixing vessel 300 to the low-pressure gas engine 500 to a temperature required by the low-pressure gas engine 500 . ); may be further provided.

FIG. 2 illustrates that the fuel control line PL2 is branched from the front end of the fuel gas heater 320 as an example. However, the above-described fuel control line PL2 may be branched from the rear end of the fuel gas heater 320 . When the fuel gas heated by the fuel gas heater 320 is supplied to the mixing container 300 as described above, the mixing ratio of the fuel gas can be adjusted by vaporizing the condensed evaporative natural gas in the mixing container 300 .

Hereinafter, a method of supplying fuel gas in which natural gas and hydrogen gas are mixed at a certain ratio to the low-pressure gas engine 500 using a fuel supply system according to an embodiment of the present invention will be described with reference to FIG. 2 . .

The evaporative natural gas from the LNG storage tank 100 is discharged along the evaporative natural gas line NL, and compressed by the natural gas compressor 110 to a low pressure, that is, to a pressure required by the low-pressure gas engine 500 . In addition, the evaporated hydrogen gas from the liquid hydrogen storage tank 200 is discharged along the evaporated hydrogen gas line HL, and the hydrogen gas compressor 210 compresses it to a low pressure, that is, a pressure required by the low pressure gas engine 500 .

The low-pressure evaporative natural gas compressed by the natural gas compressor 110 and the low-pressure evaporative hydrogen gas compressed by the hydrogen gas compressor 210 are heat-exchanged in the heat exchanger 130 . In the heat exchanger 130, the low-pressure evaporated natural gas is cooled by heat exchange, and the temperature of the low-pressure evaporated hydrogen gas is increased.

The control unit, the flow rate of fuel gas required by the low-pressure gas engine 500, the mixing ratio of the fuel gas supplied to the low-pressure gas engine 500, the temperature of evaporative natural gas or evaporative hydrogen gas at the rear end of the heat exchanger 130, The opening and closing amount of the hydrogen gas flow valve 220 and the natural gas flow valve 120 is controlled according to factors such as the flow rate and the flow rate of the evaporated natural gas to be reliquefied. By controlling the hydrogen gas flow valve 220 and the natural gas flow valve 120 , the flow rates of the low-pressure evaporative natural gas and the low-pressure evaporative hydrogen gas supplied to the heat exchanger 130 can be adjusted.

After heat exchange in the heat exchanger 130 , the evaporated hydrogen gas having an increased temperature is supplied to the mixing vessel 300 .

The low-pressure evaporative natural gas cooled by heat exchange in the heat exchanger 130 is supplied to the gas-liquid separator 140 to separate the reliquefied evaporative natural gas from the non-reliquefied evaporative natural gas. The reliquefied evaporative natural gas in the liquid state separated by the gas-liquid separator 140 is recovered to the LNG storage tank 100 , and the vaporized natural gas in the gaseous state that is not reliquefied is supplied to the mixing vessel 300 .

In the mixing container 300 , the evaporated natural gas and the evaporated hydrogen gas supplied to the mixing container 300 are uniformly mixed. At this time, the control unit maintains a constant mixing ratio of the evaporative natural gas and the evaporative hydrogen gas by adjusting the flow rates of the evaporative natural gas and the evaporative hydrogen gas supplied to the mixing vessel 300, or may adjust the mixing ratio as necessary. .

In the mixing container 300 , the fuel gas in which the evaporated natural gas and the evaporated hydrogen gas are uniformly mixed according to the mixing ratio is discharged from the mixing container 300 along the low pressure fuel gas line FL2 , and in the fuel gas heater 320 . It is heated to a temperature required by the low-pressure gas engine 500 and supplied as fuel for the low-pressure gas engine 500 .

In the mixing container 300 , only gaseous fuel gas is supplied to the fuel gas heater 320 , and the condensed and evaporated natural gas in the condensed liquid state is separately discharged and recovered to the LNG storage tank 100 .

The control unit is supplied from the mixing vessel 300 to the low-pressure gas engine 500 according to the flow rate of evaporative natural gas to be recovered to the LNG storage tank 100 and the amount or mixing ratio of fuel gas to be supplied to the low-pressure gas engine 500 . A portion of the fuel gas may be re-supplied to the mixing vessel 300 .

By re-supplying some of the fuel gas supplied from the mixing vessel 300 to the low-pressure gas engine 500 or heated by the fuel gas heater 320 to the mixing vessel 300, a liquid state in the mixing vessel 300 By vaporizing the condensed evaporative natural gas remaining in the furnace, the mixing ratio of fuel gas supplied to the low-pressure gas engine 500 and the flow rate of the condensed evaporative natural gas recovered to the LNG storage tank 100 can be adjusted.

1 shows a fuel supply system for supplying fuel to the high-pressure gas engine 400 , and FIG. 2 shows a fuel supply system for supplying fuel to the low-pressure gas engine 500 . 1 and 2 , the fuel supply system according to the first and second embodiments of the present invention may supply fuel to the high-pressure gas engine 400 or the low-pressure gas engine 500 , respectively. However, although not shown in the drawings, both the high-pressure gas engine 400 and the low-pressure gas engine 500 are provided to simultaneously or selectively supply fuel to the high-pressure gas engine 400 and the low-pressure gas engine 500 as needed. it might be

That is, as another embodiment, referring to FIGS. 1 and 2 , both the high-pressure fuel gas line FL1 and the low-pressure fuel gas line FL2 are connected from the mixing vessel 300 , and the high-pressure fuel gas line FL1 . is provided with a fuel gas compressor 310 , and a fuel gas heater 320 is provided on the low pressure fuel gas line FL2 , respectively, from the mixing vessel 300 through the high pressure fuel gas line FL1 through the high pressure gas engine 400 . ) to supply fuel gas, and may supply fuel gas to the low pressure gas engine 500 through the low pressure fuel gas line FL2.

Next, a fuel supply system according to a third embodiment of the present invention will be described with reference to FIG. 3 .

The fuel supply system according to the third embodiment of the present invention includes all of the above-described first or second embodiment, a high-pressure gas engine 400 and a low-pressure gas engine 500 , and a high-pressure gas engine 400 and It is possible to simultaneously or selectively supply fuel gas to the low-pressure gas engine 500 , and there is a difference in that the compressed hydrogen tank 140 is provided.

Hereinafter, a third embodiment of the present invention will be described focusing on differences from the first and second embodiments. Even if a detailed description of each component or its operation is omitted, the same reference numerals may be applied in the same manner as in the first embodiment or the second embodiment, and may be modified within a design changeable range.

A fuel supply system according to a third embodiment of the present invention, as shown in Figure 3, an LNG storage tank (100); liquid hydrogen storage tank 200; heat exchanger 130 ; mixing vessel 300; high-pressure gas engine 400; and a low-pressure gas engine 500 .

The LNG storage tank 100 , the heat exchanger 130 and the mixing vessel 300 of this embodiment are connected by an evaporative natural gas line (NL), and the liquid hydrogen storage tank 200 , the heat exchanger 130 and the mixing vessel 300 is connected by an evaporation hydrogen gas line (HL).

Each of the evaporative natural gas line NL and the evaporative hydrogen gas line HL may be provided with an on/off valve. A control unit (not shown) may control the on-off valve of the evaporative natural gas line NL and the on-off valve of the evaporative hydrogen gas line HL.

The evaporative natural gas line NL of this embodiment includes a natural gas compressor 110 that compresses the evaporative natural gas to a pressure required by the low-pressure gas engine 500, or a pressure slightly higher than that in consideration of the pressure loss at the rear end; is connected with

In addition, the evaporated hydrogen gas line (HL) is a hydrogen gas compressor 210 that compresses the evaporated hydrogen gas to a pressure required by the low-pressure gas engine 500, or a pressure slightly higher than that in consideration of the pressure loss at the rear end; and connected

The low-pressure gas engine 500 of this embodiment may be a DFDE engine. Accordingly, the natural gas compressor 110 compresses the evaporative natural gas to the pressure required by the DFDE engine 500 , that is, about 2 bar to 8 bar or about 4 bar to 6.5 bar. In addition, the hydrogen gas compressor 210 compresses the evaporated hydrogen gas to the pressure required by the DFDE engine 500 , that is, about 2 bar to 8 bar, or about 4 bar to 6.5 bar.

In the heat exchanger 130 of this embodiment, the evaporative natural gas compressed to a low pressure in the natural gas compressor 110 and the evaporative hydrogen gas compressed to a low pressure in the hydrogen gas compressor 210 exchange heat exchange, Evaporated natural gas is cooled by

The low-pressure evaporative natural gas cooled in the heat exchanger 130 and the low-pressure evaporative hydrogen gas whose temperature is increased while cooling the low-pressure evaporative natural gas in the heat exchanger 130 are introduced into the mixing vessel 300, and in the mixing vessel 300 At an appropriate mixing ratio, low-pressure evaporative natural gas and low-pressure evaporative hydrogen gas are uniformly mixed.

Although not shown in the drawings, at the front end of the heat exchanger 130 , an evaporative natural gas flow control valve for controlling the flow rate of evaporative natural gas introduced into the heat exchanger 130 , and natural hydrogen gas introduced into the heat exchanger 130 . An evaporative hydrogen gas flow rate control valve for controlling the flow rate of may be provided. A control unit (not shown) controls the evaporative natural gas flow rate control valve and the evaporative hydrogen gas flow rate control valve to adjust the flow rates of the evaporative natural gas and the evaporative hydrogen gas introduced into the heat exchanger 130 .

Accordingly, it is possible to control the temperature of the evaporative natural gas and the evaporative hydrogen gas discharged after heat exchange from the heat exchanger 130, and it is possible to control the mixing ratio of the evaporative natural gas and the evaporative hydrogen gas mixed in the mixing vessel 300, , it is possible to control the amount of evaporated natural gas recovered by re-liquefaction.

According to this embodiment, a gas-liquid separator 140 for gas-liquid separation of the reliquefied evaporative natural gas and the non-reliquefied evaporative natural gas among the evaporative natural gas cooled by the cooling heat of the evaporative hydrogen gas in the heat exchanger 130; more are available

The evaporative natural gas line (NL) is connected from the gas-liquid separator 140 to the mixing vessel 300, and the evaporative natural gas in the gaseous state separated by the gas-liquid separator 140 is mixed along the evaporative natural gas line (NL) into the mixing vessel ( 300) is supplied.

In addition, the gas-liquid separator 140 is connected to a first recovery line RL1 connected from the gas-liquid separator 140 to the LNG storage tank 100 . The liquid reliquefied natural gas separated in the gas-liquid separator 140 is recovered to the LNG storage tank 100 along the first recovery line RL1.

An opening/closing valve may be provided in the first recovery line RL. The controller may control the opening/closing valve of the first recovery line RL1 to recover the reliquefied natural gas from the gas-liquid separator 140 to the LNG storage tank 100 .

For example, when the water level level in the gas-liquid separator 140 reaches a set value, the control unit opens the opening/closing valve of the first recovery line RL1 according to the operation mode to remove the LNG storage tank 100 from the gas-liquid separator 140 . to allow the flow of reliquefied natural gas.

In addition, the control unit, the amount of evaporative natural gas is large compared to the amount of fuel gas required by the engines 400 and 500, or lowering the ratio of the evaporative natural gas among the mixing ratio of the fuel gas mixed in the mixing vessel 300 In order to condense a larger amount of evaporative natural gas, a greater amount of evaporative natural gas is reliquefied in the gas-liquid separator 140 by controlling the flow rates of evaporative hydrogen gas and evaporative natural gas introduced into the heat exchanger 130 . You can even control it as much as possible.

According to this embodiment, the first evaporative natural gas branched from the evaporative natural gas line NL so that the low-pressure BOG compressed in the natural gas compressor 110 bypasses the heat exchanger 130 and is introduced into the mixing vessel 300 . A branch line NL1 may be further provided.

The first evaporative natural gas branch line NL1 is branched from the evaporative natural gas line NL at the front end of the heat exchanger 130 and may be connected to the front end of the mixing vessel 300, more specifically, the front end flow of the gas-liquid separator 140. there is.

An on-off valve may be provided in the first evaporative natural gas branch line NL1. The control unit controls the on-off valve to introduce some of the low-pressure evaporative natural gas compressed in the natural gas compressor 110 into the first evaporative natural gas branch line NL1 to bypass the heat exchanger 130 .

The mixing vessel 300 of this embodiment is connected from the LNG storage tank 100 and includes an evaporative natural gas line (NL) through which the evaporative natural gas flows from the LNG storage tank 100 to the mixing vessel 300 ; and an evaporated hydrogen gas line (HL) connected from the liquid hydrogen storage tank 200 and through which the evaporated hydrogen gas flows from the liquid hydrogen storage tank 200 to the mixing vessel 300; is connected. The mixing vessel 300 supplies a fuel gas obtained by uniformly mixing the evaporated natural gas and the evaporated hydrogen gas as the fuel of the engines 400 and 500 .

The control unit may control the flow rate of the evaporative natural gas supplied to the mixing vessel 300 by measuring the flow rate of the evaporative natural gas supplied to the mixing vessel 300 and adjusting the opening and closing of the natural gas flow valve.

In addition, the controller may control the flow rate of the evaporated hydrogen gas supplied to the mixing vessel 300 by measuring the flow rate of the evaporated hydrogen gas supplied to the mixing vessel 300 and adjusting the opening and closing of the hydrogen gas flow valve.

Therefore, according to the present embodiment, the flow rate of the evaporative natural gas and the evaporative hydrogen gas supplied to the mixing vessel 300 is controlled to adjust the natural gas and hydrogen gas mixing ratio of the fuel gas to be supplied as the fuel of the engines 400 and 500 . can

The mixing ratio of the fuel gas to be mixed in the mixing vessel 300 may be a preset value or may be changed in real time according to the operating state of the vessel.

In addition, the mixing vessel 300 of this embodiment is connected to the high-pressure gas engine 400 and the fuel gas mixed in the mixing vessel 300 flows from the mixing vessel 300 to the high-pressure gas engine 400 . line FL1; a low pressure fuel gas line (FL2) connected to the low pressure gas engine 500 and flowing from the mixing vessel 300 to the low pressure gas engine 500 through which the fuel gas mixed in the mixing vessel 300 flows; and a second recovery line RL2 connected to the LNG storage tank 100 and in which the condensate condensed in the mixing vessel 300 flows from the mixing vessel 300 to the LNG storage tank 100; is connected.

The flow rate of fuel gas supplied from the mixing vessel 300 to the high-pressure gas engine 400 along the high-pressure fuel gas line FL1 may be adjusted according to the amount of fuel gas required by the high-pressure gas engine 400 .

In addition, the flow rate of fuel gas supplied from the mixing vessel 300 to the low pressure gas engine 500 along the low pressure fuel gas line FL2 may be adjusted according to the amount of fuel gas required by the low pressure gas engine 500 . there is.

In the high-pressure fuel gas line FL1 of this embodiment, a fuel gas compressor 310 for compressing the fuel gas supplied from the mixing vessel 300 to the high-pressure gas engine 400 to the high pressure required by the high-pressure gas engine 400; is provided

The high-pressure gas engine 400 of this embodiment may mix natural gas and hydrogen gas, for example, it may be a ME-GI engine (MAN Electronic Gas Injection Engine). Accordingly, the fuel gas compressor 310 of the present embodiment may compress the fuel gas to about 100 bar to 400 bar, or about 150 bar to 300 bar.

In addition, the low-pressure fuel gas line FL2 of this embodiment is connected from the mixing vessel 300 to the low-pressure gas engine 500 . The fuel gas supplied to the low-pressure gas engine 500 through the low-pressure fuel gas line FL2 is discharged from the mixing vessel 300 and supplied to the low-pressure gas engine 500 without additional compression.

3 to 6, the low-pressure fuel gas line FL2 is branched from the high-pressure fuel gas line FL1, and the fuel gas flowing along the low-pressure fuel gas line FL2 is connected to bypass the fuel gas compressor 310, there is. However, the present invention is not limited thereto, and the low-pressure fuel gas line FL2 may be separately connected from the mixing vessel 300 to the low-pressure gas engine 500 .

In addition, although not shown in the drawings, the low-pressure fuel gas line FL2 may further include a fuel gas heater for heating the fuel gas to a temperature required by the low-pressure gas engine 500 .

According to the embodiment, some of the fuel gas supplied from the mixing vessel 300 to the engines 400 and 500 along the high-pressure fuel gas line FL1 or the low-pressure fuel gas line FL2 is re-supplied to the mixing vessel 300 . A fuel control line PL branched from the high-pressure fuel gas line FL1 or the low-pressure fuel gas line FL2 may be further provided.

The fuel control line PL is provided with an on/off valve, and the controller controls the on/off valve so that some of the fuel gas supplied from the mixing vessel 300 to the engines 400 and 500 is supplied back to the mixing vessel 300 . can

The control unit, to adjust the water level or pressure in the mixing vessel 300, to adjust the mixing ratio of natural gas and hydrogen gas, or to adjust the flow rate of fuel gas supplied to the engines (400, 500) , a part of the fuel gas may be re-supplied to the mixing vessel 300 along the high-pressure fuel gas line FL1 or the low-pressure fuel gas line FL2 by controlling the on-off valve of the fuel control line PL.

In addition, the controller may re-supply some of the fuel gas supplied to the engines 400 and 500 to the mixing vessel 300 to vaporize the condensate in the mixing vessel 300 .

For example, by re-supplying some of the fuel gas compressed by the fuel gas compressor 310 to the mixing container 300 , the control unit uses the fuel gas whose temperature is increased by compression in the fuel gas compressor 310 into the mixing container. (300) It is also possible to vaporize the condensate.

According to the present embodiment, the first evaporative hydrogen gas branch line HL1 branched from the evaporative hydrogen gas line HL so that some or all of the evaporative hydrogen gas supplied to the mixing vessel 300 is supplied to the fuel gas compressor 310 . ); and a compressed hydrogen tank 240 for storing compressed hydrogen gas compressed to a high pressure in the fuel gas compressor 310; may further include.

The first evaporative hydrogen gas branch line HL1 may be branched from the rear end of the heat exchanger 130 and connected to the front end of the fuel gas compressor 310 as shown in FIGS. 3 to 6 . That is, the high-pressure evaporated hydrogen gas compressed by the hydrogen gas compressor 210 at a low pressure and heat exchanged in the heat exchanger 130 and then compressed by the fuel gas compressor 310 may be stored in the compressed hydrogen tank 240 .

However, the present invention is not limited thereto, and for example, evaporated hydrogen gas may be directly introduced into the fuel gas compressor 310 without heat exchange in the heat exchanger 130 .

The first evaporative hydrogen gas branch line (HL1) is provided with an on/off valve, and the control unit controls the on-off valve of the first evaporative hydrogen gas branch line (HL1) so that the evaporative hydrogen gas is supplied to the fuel gas compressor (310). can

For example, when the amount of evaporative hydrogen gas is greater than the mixing ratio of the fuel gas mixed in the set mixing container 300, the control unit opens the opening/closing valve of the first evaporative hydrogen gas branch line HL1, Some or all of the gas may be supplied to the fuel gas compressor 310 .

As described above, the fuel gas compressor 310 may compress the gas to about 100 bar to 400 bar. The evaporated hydrogen gas compressed in the fuel gas compressor 310 is branched from the high-pressure fuel gas line FL1 at the rear end of the fuel gas compressor 310 and flows along the hydrogen storage line SL connected to the compressed hydrogen tank 240 . to be supplied to the compressed hydrogen tank 240 .

The compressed hydrogen tank 240 may be a compression container capable of storing the evaporated hydrogen gas compressed at high pressure. According to the present embodiment, since the evaporated hydrogen gas stored in the compressed hydrogen tank 240 is compressed and stored at a high pressure in the fuel gas compressor 310, the compressed hydrogen tank 240 has a structure that can withstand the pressure of the evaporated hydrogen gas. can have

3 shows that three compressed hydrogen tanks 240 are provided as an example. However, the present invention is not limited thereto.

The high-pressure evaporated hydrogen gas stored in the compressed hydrogen tank 240 is a hydrogen storage line (SL) connected from the compressed hydrogen tank 240 to the high-pressure fuel gas line (FL1) or the low-pressure fuel gas line (FL2) according to the operation mode. It flows along and is mixed with the fuel gas supplied to the engines 400 and 500 and may be supplied as the fuel of the engines 400 and 500 .

Hereinafter, a method of operating a fuel supply system according to a third embodiment of the present invention will be described with reference to FIGS. 4 to 6 . In the operating method of the fuel supply system to be described later, it will be described as an embodiment that the operation is divided into three operation modes, but the present invention is not limited thereto, and it is obvious that the fuel supply system may be changed within a design change range.

4 to 6, the flow of the fluid is indicated by a thick solid line and a thick dotted line. This indicates only the main flow of the fluid for convenience of description, and the fluid does not necessarily flow only in the same manner as shown in the drawings in the corresponding operation mode. For example, although the second recovery line RL2 is shown as a solid line in FIG. 4 , this may not necessarily mean that the evaporated natural gas is not recovered by reliquefying it in the first operation mode.

In addition, the high-pressure gas engine 400, a ME-GI engine, may be used as a propulsion engine of a ship, and the low-pressure gas engine 500, a DFDE engine, may be used as an engine for power generation of a ship.

First, a method of operating the fuel supply system in the first operation mode according to the third embodiment of the present invention will be described with reference to FIG. 4 .

The first operation mode of this embodiment is a high-pressure gas engine 400 by uniformly mixing the evaporated natural gas generated in the LNG storage tank 100 and the evaporated hydrogen gas generated in the liquid hydrogen storage tank 100 at a certain ratio. supplied as fuel for The first operation mode may be used during general navigation of the vessel.

In the first operation mode, the evaporated hydrogen gas discharged from the liquid hydrogen storage tank 200 is compressed to a low pressure in the hydrogen gas compressor 120 , and the compressed low pressure evaporated hydrogen gas is low pressure evaporated natural gas in the heat exchanger 130 . heat exchange with In the heat exchanger 130 , the low-pressure evaporative hydrogen gas, whose temperature is increased by heat exchange with the low-pressure evaporative natural gas, is supplied to the mixing vessel 300 .

The evaporative natural gas discharged from the LNG storage tank 100 is compressed to a low pressure in the natural gas compressor 110 , and the compressed low-pressure evaporative natural gas is cooled by using the cooling heat of the low-pressure evaporative hydrogen gas in the heat exchanger 130 . .

A portion of the low-pressure evaporative hydrogen gas cooled by heat exchange with the low-pressure evaporative hydrogen gas in the heat exchanger 130 may be liquefied by heat exchange.

The reliquefied BOG liquefied by heat exchange is gas-liquid separated in the gas-liquid separator 140, and the liquid reliquefied BOG is recovered to the LNG storage tank 100, and the low-pressure evaporative natural gas in the cooled gaseous state is not reliquefied. The gas is supplied to the mixing vessel 300 .

In this case, the controller may adjust the amount of the evaporated natural gas to be reliquefied by adjusting the flow rates of the evaporated hydrogen gas and the evaporated natural gas supplied to the heat exchanger 130 . For example, if the amount of evaporative natural gas is greater than the amount of fuel gas required by the high-pressure gas engine 400, or the amount of evaporative natural gas is large compared to the amount of evaporative hydrogen gas, mixing in the mixing vessel 300 as it is If the appropriate mixing ratio cannot be satisfied, the control unit may adjust the flow rate so that the amount of the evaporated natural gas to be reliquefied is large.

In the mixing vessel 300 , the evaporated hydrogen gas and the evaporated natural gas are uniformly mixed, and the fuel gas mixed according to the mixing ratio set by the control unit is the high pressure required by the high-pressure gas engine 400 in the fuel gas compressor 310 . is compressed and supplied as fuel of the high-pressure gas engine 400 .

The high-pressure gas engine 400 burns fuel gas in which evaporative natural gas and evaporative hydrogen gas are mixed in a certain ratio to generate propulsion energy for the ship, and fuel gas in which evaporative natural gas and evaporative hydrogen gas are mixed in a certain ratio is used as fuel. As a result, the amount of nitrogen oxide and carbon dioxide produced in exhaust gas is reduced.

At this time, the control unit, by controlling the flow rates of the evaporated hydrogen gas and the evaporated natural gas supplied to the mixing vessel 300, it is possible to match the mixing ratio. Alternatively, some of the fuel gas compressed by the fuel gas compressor 310 may be supplied back to the mixing container 300 to vaporize the condensate in the mixing container 300 , thereby controlling the mixing ratio to be adjusted.

The condensate condensed in the mixing vessel 300 is evaporative natural gas having a higher boiling point than evaporative hydrogen gas, and the condensate in the mixing vessel 300 may be recovered to the LNG storage tank 100 if necessary.

When a demand for fuel gas occurs in the low-pressure gas engine 500, the amount of fuel gas required by the low-pressure gas engine 500 among the remaining fuel gas after supplying it from the mixing vessel 300 to the high-pressure gas engine 400 is fuel gas. By bypassing the compressor 310 , it may be supplied as fuel for the low-pressure gas engine 500 .

Next, an operating method of the second operation mode of the fuel supply system according to the third embodiment of the present invention will be described with reference to FIG. 5 .

The second operation mode of the present embodiment may be used when the ship is unloading liquid cargo. In particular, the second mode of operation may be used during liquid hydrogen unloading of a vessel. When liquid hydrogen is unloaded, a large amount of evaporated hydrogen gas is generated, and the second operation mode according to the present embodiment can effectively process such a large amount of evaporated hydrogen gas.

In the second operation mode, the evaporative natural gas generated in the LNG storage tank 100 is supplied as fuel of the low-pressure gas engine 500 , and the evaporative hydrogen gas generated in the liquid hydrogen storage tank 200 is converted into a compressed hydrogen tank 240 . ) is stored in

When the ship is unloading liquid cargo, the propulsion engine, that is, the high-pressure gas engine 400 is not operated, and only the power generation engine, that is, the low-pressure gas engine 500 is operated, and in the second operation mode, the evaporated natural gas is converted into the low-pressure gas engine. (500) of fuel is supplied.

In addition, although the evaporation hydrogen gas is stored in the compressed hydrogen tank 240 as an example in this embodiment, some of the evaporated hydrogen gas is supplied to the mixing vessel 300 and uniformly mixed with the evaporated natural gas at a certain ratio. After being supplied to the low-pressure gas engine 500 , the remaining evaporated hydrogen gas may be stored in the compressed hydrogen tank 240 after being supplied as fuel of the low-pressure gas engine 500 .

The evaporated hydrogen gas discharged from the liquid hydrogen storage tank 200 is compressed to a low pressure in the hydrogen gas compressor 120 , and the compressed low-pressure evaporated hydrogen gas is heat-exchanged with the low-pressure evaporated natural gas in the heat exchanger 130 . In the heat exchanger 130 , the temperature of the low-pressure evaporative hydrogen gas increases by heat exchange with the low-pressure evaporative natural gas.

Evaporated hydrogen gas discharged after heat exchange in the heat exchanger 130 is compressed to a high pressure in the fuel gas compressor 310 and stored in the compressed hydrogen tank 240 .

The evaporative natural gas generated in the LNG storage tank 100 is compressed by the natural gas compressor 110 to the low pressure required by the low-pressure gas engine 500 , and the compressed low-pressure evaporative natural gas is evaporated at a low pressure in the heat exchanger 130 . It is cooled using the cooling heat of hydrogen gas.

A portion of the low-pressure evaporative hydrogen gas cooled by heat exchange with the low-pressure evaporative hydrogen gas in the heat exchanger 130 may be liquefied by heat exchange.

The reliquefied BOG liquefied by heat exchange is gas-liquid separated in the gas-liquid separator 140, and the liquid reliquefied BOG is recovered to the LNG storage tank 100, and the low-pressure evaporative natural gas in the cooled gaseous state is not reliquefied. The gas is supplied as a fuel of the low-pressure gas engine 500 .

The low-pressure evaporative natural gas in the gaseous state may be supplied to the low-pressure gas engine 500 through the mixing vessel 300 , and although not shown in the drawing, a separate piping line bypassing the mixing vessel 300 is further provided to provide a low pressure It may be supplied to the gas engine 500 . When the low-pressure evaporative natural gas passes through the mixing vessel 300 and is supplied to the low-pressure gas engine 500 , the mixing vessel 300 may serve as a buffer tank.

In the drawing, although it is illustrated as an example that all of the low-pressure evaporated hydrogen gas discharged after heat exchange in the heat exchanger 130 is stored in the compressed hydrogen tank 240 , some of the evaporated hydrogen gas is supplied to the mixing vessel 300 and mixed. The remaining low pressure evaporated hydrogen gas supplied to the container 300 may be compressed to a high pressure in the fuel gas compressor 310 and stored in the compressed hydrogen tank 240 .

At this time, the low-pressure evaporative hydrogen gas and the low-pressure evaporative natural gas are uniformly mixed at an appropriate mixing ratio in the mixing vessel 300 and supplied as fuel for the low-pressure gas engine 500 .

Next, an operating method of the third operation mode of the fuel supply system according to the third embodiment of the present invention will be described with reference to FIG. 6 .

The third operation mode of the present embodiment may be used when the vessel is unloading liquid cargo and the liquid cargo storage tank is empty or is maintained below the minimum water level. In particular, it can be used when a liquid hydrogen carrier unloads liquid hydrogen at a loading dock and returns to a supply station. At this time, although the high-pressure gas engine 400 is operated for the operation of the vessel, there is little or no evaporated hydrogen gas generated in the liquid hydrogen storage tank 200 . Therefore, according to the third operation mode of the present embodiment, even in this case, the fuel gas obtained by mixing the evaporative natural gas and the evaporative hydrogen gas can be supplied as a fuel to the high-pressure gas engine 400 .

According to this embodiment, the evaporated natural gas generated in the LNG storage tank 100 and the hydrogen gas stored in the compressed hydrogen tank 240 in the second operation mode are mixed and supplied as fuel of the high-pressure gas engine 400 .

The evaporative natural gas discharged from the LNG storage tank 100 is compressed to a low pressure by the natural gas compressor 110 , and the compressed low-pressure evaporative natural gas is the high pressure required by the high-pressure gas engine 400 by the fuel gas compressor 310 . is compressed and supplied as fuel of the high-pressure gas engine 400 .

At this time, the high-pressure evaporative natural gas supplied to the high-pressure gas engine 400 is mixed with the compressed hydrogen gas stored in the compressed hydrogen tank 240, and the fuel gas obtained by mixing the high-pressure evaporative natural gas and the compressed hydrogen gas is mixed with the high-pressure gas engine ( 400) is supplied.

As described above, according to the present invention, as a mixed combustion engine of natural gas and hydrogen gas, by supplying a mixture of natural gas and hydrogen gas as fuel for the engine, it is possible to reduce the amount of nitrogen oxide and carbon dioxide produced. In particular, the combustion safety of the engine can be improved by uniformly mixing natural gas and hydrogen gas at an appropriate mixing ratio in the mixing container and supplying the fuel as fuel.

In addition, since a part of evaporative natural gas can be reliquefied by the cooling and heat of hydrogen gas, even if excess evaporative natural gas is generated, it can be recovered in a liquid state in the LNG storage tank.

In addition, when evaporated hydrogen gas is generated in excess, hydrogen has a very low boiling point, making it difficult to reliquefy, and the hydrogen reliquefaction system has very high installation and operating costs. However, according to the present invention, the excess evaporative hydrogen gas is compressed using a fuel gas compressor and stored in a compressed hydrogen tank, so that hydrogen gas can be used when needed, thereby reducing unnecessary waste of hydrogen.

It is apparent to those of ordinary skill in the art that the present invention is not limited to the above embodiments, and that various modifications or variations can be implemented without departing from the technical gist of the present invention. did it

100: LNG storage tank
200: liquid hydrogen storage tank
300: mixing vessel
240: compressed hydrogen tank
400: high pressure gas engine
500: low pressure gas engine
110: natural gas compressor
210: hydrogen gas compressor
130: heat exchanger
140: gas-liquid separator
310: fuel gas compressor
120: natural gas flow valve
220: hydrogen gas flow valve
NL : Evaporated Natural Gas Line
HL : Evaporated hydrogen gas line
HL1: 1st evaporative hydrogen gas branch line
RL1: first recovery line
RL2: second recovery line
PL: fuel control line
FL1 : High-pressure fuel gas line
FL2 : Low pressure fuel gas line
SL : Hydrogen storage line

Claims (15)

an engine for mixing liquefied gas and hydrogen gas;
a mixing vessel for generating fuel gas by mixing vaporized liquefied gas and vaporized hydrogen gas;
a fuel gas compressor for compressing the fuel gas supplied to the engine to a pressure required by the engine; and
Including; a compressed hydrogen tank for compressing and storing the surplus evaporated hydrogen gas in the fuel gas compressor;
The fuel gas generated in the mixing container is supplied as a fuel of the engine, and the evaporated hydrogen gas remaining after supplying it as the fuel of the engine is stored in the compressed hydrogen tank,
a fuel control line re-supplying some of the fuel gas compressed in the fuel gas compressor to the mixing vessel; and
Further comprising; a control unit for controlling the on-off valve of the fuel control line to adjust the mixing ratio of the fuel gas mixed in the mixing vessel;
The control unit opens the fuel control line to vaporize the condensate in the mixing vessel, the fuel supply system of the vessel. The method according to claim 1,
and a hydrogen storage line connecting the compressed hydrogen tank and the engine, and mixing the compressed hydrogen gas stored in the compressed hydrogen tank with the fuel gas supplied to the engine. The method according to claim 1 or 2,
The engine is
a low-pressure gas engine using low-pressure fuel gas as a fuel; and
A high-pressure gas engine using high-pressure fuel gas as a fuel;
The fuel gas compressor is capable of compressing fuel gas to a pressure required by the high-pressure gas engine, a fuel supply system for a ship. 4. The method according to claim 3,
a heat exchanger for cooling the vaporized liquefied gas by exchanging the vaporized liquefied gas with the vaporized hydrogen gas; and
Further comprising; a gas-liquid separator for gas-liquid separation of the evaporative liquefied gas reliquefied by the cooling heat of the evaporative hydrogen gas in the heat exchanger and the evaporative liquefied gas that is not reliquefied,
The vaporized liquefied gas in the gaseous state separated in the gas-liquid separator is supplied to the mixing vessel,
The reliquefaction evaporation liquefied gas in the liquid state separated in the gas-liquid separator is recovered to the liquefied gas storage tank, the fuel supply system of the ship. 5. The method according to claim 4,
a hydrogen gas flow valve for controlling a flow rate of evaporated hydrogen gas supplied to the heat exchanger;
a liquefied gas flow valve for controlling the flow rate of evaporative liquefied gas supplied to the heat exchanger; and
A control unit for controlling a mixing ratio of the fuel gas mixed in the mixing vessel by controlling the hydrogen gas flow valve and the liquefied gas flow valve; further comprising, a fuel supply system for a ship. 5. The method according to claim 4,
a hydrogen gas compressor for compressing the evaporated hydrogen gas supplied to the heat exchanger to a pressure required by the low-pressure gas engine; and
Further comprising; a liquefied gas compressor for compressing the evaporative liquefied gas supplied to the heat exchanger to the pressure required by the low-pressure gas engine;
The low-pressure evaporative hydrogen gas compressed by the hydrogen gas compressor and the low-pressure evaporative liquefied gas compressed by the liquefied gas compressor are supplied to the heat exchanger, a fuel supply system for a ship. 5. The method according to claim 4,
A second recovery line for recovering the condensate condensed in the mixing container to the liquefied gas storage tank; further comprising, a fuel supply system for a ship. delete In the fuel supply method of a ship comprising a liquid hydrogen storage tank and a liquid hydrogen storage tank,
Compressing the evaporated liquefied gas generated in the liquid hydrogen storage tank and the evaporated hydrogen gas generated in the liquid hydrogen storage tank, respectively,
Cooling the evaporative liquefied gas by heat-exchanging the evaporative liquefied gas and the evaporating hydrogen gas in a heat exchanger,
Supplying a fuel gas obtained by mixing the evaporated hydrogen gas whose temperature is increased by the heat exchange and the evaporative liquefied gas cooled by the heat exchange as fuel of the engine,
The evaporated hydrogen gas remaining after being supplied as the fuel is further compressed and stored in a compressed hydrogen tank,
When the evaporated hydrogen gas generated from the liquid hydrogen storage tank is insufficient,
A method of supplying a fuel for a ship by mixing the stored evaporative hydrogen gas and the evaporative liquefied gas as fuel for a high-pressure gas engine. 10. The method of claim 9,
The evaporated liquefied gas reliquefied by the heat exchange is recovered to a liquefied gas storage tank,
A method of supplying a fuel for a ship by mixing the evaporated hydrogen gas with the vaporized liquefied gas in a gaseous state that is not reliquefied by the heat exchange as fuel for the engine. 10. The method of claim 9,
A method for supplying fuel to a ship, controlling a flow rate of evaporative liquefied gas supplied to the heat exchanger and evaporative hydrogen gas supplied to the heat exchanger to adjust a mixing ratio of the fuel gas. 10. The method of claim 9,
The fuel gas is supplied to a fuel gas compressor and compressed to the high pressure required by the high-pressure gas engine,
A method of supplying fuel gas compressed to a high pressure to the high-pressure gas engine, a fuel supply method for a ship. 13. The method of claim 12,
The evaporative liquefied gas and the evaporative hydrogen gas supplied to the heat exchanger are compressed to a low pressure required by the low-pressure gas engine, respectively,
A fuel supply method for a ship, wherein the fuel gas obtained by mixing the evaporated liquefied gas and the evaporated hydrogen gas compressed to the low pressure after heat exchange is supplied to the low-pressure gas engine. 14. The method of claim 13,
When the high-pressure gas engine is not operated and only the low-pressure gas engine is operated,
supplying the fuel gas as a fuel of the low-pressure gas engine,
The surplus evaporated hydrogen gas is compressed and stored in the fuel gas compressor, a fuel supply method for a ship. delete

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