KR101910713B1 - Vessel having Gas Treatment System - Google Patents

Abstract

A ship including a gas treatment system according to an embodiment of the present invention includes a propulsion engine that receives liquefied gas from a liquefied gas storage tank and generates propulsion power of the ship; A power generation engine for generating power used in the ship; A liquefaction device for re-liquefying evaporated gas generated in the liquefied gas storage tank; And an evaporation gas sucking unit for sucking and discharging the evaporation gas generated in the liquefied gas storage tank, wherein the evaporation gas sucking unit supplies the evaporating gas to be discharged to the refill liquefier, And is not supplied to the power generation engine.

Description

[0001] VESSEL Having Gas Treatment System [0002]

The present invention relates to a vessel comprising a gas treatment system.

Liquefied natural gas (Liquefied natural gas), Liquefied petroleum gas (Liquefied petroleum gas) and other liquefied gas are widely used in place of gasoline or diesel in recent technology development.

Liquefied natural gas is a liquefied natural gas obtained by refining natural gas collected from a gas field. It is a colorless and transparent liquid with almost no pollutants and high calorific value. It is an excellent fuel. On the other hand, liquefied petroleum gas is a liquid fuel made by compressing gas containing propane (C3H8) and butane (C4H10), which come from oil in oil field, at room temperature. Liquefied petroleum gas, like liquefied natural gas, is colorless and odorless and is widely used as fuel for household, business, industrial, and automotive use.

Such liquefied gas is stored in a liquefied gas storage tank installed on the ground or stored in a liquefied gas storage tank provided in a ship which is a means of transporting the ocean. The liquefied natural gas is liquefied to a volume of 1/600 The liquefaction of liquefied petroleum gas has the advantage of reducing the volume of propane to 1/260 and the content of butane to 1/230, resulting in high storage efficiency. The temperature and pressure necessary for driving the engine using such liquefied gas as fuel may be different from the state of the liquefied gas stored in the tank.

In addition, when LNG is stored in a liquid state, some LNG is vaporized and boil off gas (BOG) is generated as heat penetration occurs in the tank. Such evaporation gas may cause problems in a liquefied gas processing system. In order to solve the problem by discharging the evaporation gas to the outside (in the past, the evaporation gas was simply discharged to the outside in order to lower the tank pressure by lowering the tank pressure), the problem was solved. However, .

 In recent years, researches and developments have been actively conducted on utilization methods such as recycling the generated evaporated gas through a liquefied gas, liquefying it, and supplying it to the engine as a technique for efficiently processing the evaporated gas.

SUMMARY OF THE INVENTION The present invention has been made to improve the prior art, and it is an object of the present invention to provide a vessel including a gas treatment system that effectively supplies liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer.

A ship including a gas treatment system according to an embodiment of the present invention includes a propulsion engine that receives liquefied gas from a liquefied gas storage tank and generates propulsion power of the ship; A power generation engine for generating power used in the ship; A liquefaction device for re-liquefying evaporated gas generated in the liquefied gas storage tank; And an evaporation gas sucking unit for sucking and discharging the evaporation gas generated in the liquefied gas storage tank, wherein the evaporation gas sucking unit supplies the evaporating gas to be discharged to the refill liquefier, And is not supplied to the power generation engine.

A liquefied gas supply line connecting the liquefied gas storage tank and the propulsion engine; A pump provided on the liquefied gas supply line for pressurizing the liquefied gas stored in the liquefied gas storage tank; A vaporizer provided on the liquefied gas supply line for supplying a pressurized liquefied gas from the pump and vaporizing the liquefied gas; A driving fluid supply line branched at the rear end of the vaporizer on the liquefied gas supply line and connected to the evaporation gas suction unit; An evaporation gas suction line connecting the liquefied gas storage tank and the evaporation gas suction unit; And an evaporation gas supply line connecting the evaporation gas inlet unit and the refill liquefier.

Specifically, the propulsion engine is a high pressure gas injection engine (MEGI) that consumes 200-400 bar of vaporized liquefied gas that is pressurized from the pump and the power generation engine is a heterogeneous fuel engine that consumes 6 bar to 10 bar of evaporative gas .

Specifically, the evaporation gas sucking unit is supplied with vaporized liquefied gas of 200 to 400 bar through the driving fluid supply line, and evaporation gas of 1 to 1.06 bar generated in the liquefied gas storage tank through the evaporation gas suction line And a mixed fluid obtained by mixing the vaporized liquefied gas and the evaporated gas may be discharged at 3 to 5 bar and supplied to the remelting device.

The apparatus further comprises a quench cooler provided between the evaporation gas suction unit on the evaporation gas supply line and the refill liquefaction device for exchanging heat between the liquefied gas supplied from the pump and the mixed fluid supplied from the evaporation gas suction unit .

Specifically, the liquefied gas supply line may be provided to pass through the precooler.

Specifically, the evaporation gas supply line may be provided via the vaporizer.

Specifically, the refill liquefying apparatus may be supplied to the liquefied gas storage tank by re-liquefying the entire amount of the evaporative gas discharged from the evaporative gas suction unit through another refrigerant.

A return line connecting the liquefaction device and the liquefied gas storage tank; And a gas-liquid separator provided on the return line and separating the liquefied evaporated gas supplied from the reslurrying device into a gas phase and a liquid phase.

Specifically, the apparatus may further include a shaft generator connected to a drive shaft of the propulsion engine and generating power by at least partially receiving power generated by the propulsion engine, wherein the power generated by the shaft generator may be supplied to the re- have.

Specifically, the power generation engine can supply the generated power to the remelting device.

Specifically, the propulsion engine is a low pressure gas injection engine (XDF), and the power generation engine may be a heterogeneous fuel engine consuming 6 to 10 bar of evaporative gas.

The vessel including the gas treatment system according to the present invention has an effect of effectively supplying liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer, thereby enhancing system stability and reliability.

1 is a conceptual diagram of a gas processing system according to a first embodiment of the present invention.
2 is a conceptual diagram of a gas processing system according to a second embodiment of the present invention.
3 is a conceptual diagram of a gas processing system according to a third embodiment of the present invention.
4 is a conceptual diagram of a gas processing system according to a fourth embodiment of the present invention.
5 is a conceptual diagram of a gas processing system according to a fifth embodiment of the present invention.
6 is a conceptual diagram of a gas processing system according to a sixth embodiment of the present invention.
7 is a conceptual diagram of a gas processing system according to a seventh embodiment of the present invention.
8 is a conceptual diagram of a gas processing system according to an eighth embodiment of the present invention.
9 is a conceptual diagram of a gas processing system according to a ninth embodiment of the present invention.
10 is a conceptual diagram of a gas processing system according to a tenth embodiment of the present invention.

BRIEF DESCRIPTION OF THE DRAWINGS The objects, particular advantages and novel features of the present invention will become more apparent from the following detailed description taken in conjunction with the accompanying drawings, in which: FIG. It should be noted that, in the present specification, the reference numerals are added to the constituent elements of the drawings, and the same constituent elements are assigned the same number as much as possible even if they are displayed on different drawings. In the following description, well-known functions or constructions are not described in detail since they would obscure the invention in unnecessary detail.

Hereinafter, the liquefied gas may be LPG, LNG, or ethane, and may be, for example, LNG (Liquefied Natural Gas), and the evaporation gas may refer to BOG (Boil Off Gas) such as natural vaporized LNG.

The liquefied gas can be referred to irrespective of the state change, such as liquid state, gas state, mixed state of liquid and gas, supercooled state, supercritical state, and the like. Further, it is apparent that the present invention is not limited to the liquefied gas to be treated, but may be a liquefied gas processing system and / or an evaporative gas processing system, and the systems of the following drawings may be applied to each other. In addition, the mixed fluid described below may be a mixed vaporized gas or a fluid containing at least a part of the liquid phase.

Further, the embodiments of the gas treatment system 2 of the present invention may be configured in combination with each other, and the addition of the respective structures may be made to be an intersection with each other. The gas treatment system 2 according to an embodiment of the present invention may be mounted on the hull H and the vessel 1 may be a ship such as an LNG carrier, a container carrier, or the like, but is not limited thereto.

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

1 is a conceptual diagram of a gas processing system according to a first embodiment of the present invention.

1, the gas processing system 1 according to the first embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, a power generation engine 32, an evaporation gas suction unit 41, a refueling device 51, a gas-liquid separator 60, and a shaft generator 71.

Prior to describing the individual configurations of the gas processing system 1 according to the first embodiment of the present invention, the basic flow paths for organically connecting the individual configurations will be described. Here, the passage is a passage through which the fluid flows, and may be a line. However, the present invention is not limited thereto.

In the first embodiment of the present invention, the liquefied gas supply line L1, the driving fluid supply line L2, the first branch line L3 of the evaporation gas, the evaporation gas suction line L4, the evaporation gas supply line L5, , A first return line (L6), and a second return line (L7). Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The liquefied gas supply line L1 connects the liquefied gas storage tank 20 and the propulsion engine 31 and can include a boosting pump 21, a high pressure pump 22, a vaporizer 23, The liquefied gas stored in the storage tank 20 can be pressurized by the pumps 21 and 22 and heated by the carburetor 23 and then supplied to the propulsion engine 31. [

The driving fluid supply line L2 is branched between the vaporizer 23 and the propulsion engine 31 on the liquefied gas supply line L1 to connect the evaporation gas suction unit 41, The liquefied gas can be supplied to the evaporation gas sucking unit 41 so as to be used as a driving fluid for the evaporation gas sucking unit 41.

The first branch line L3 of the evaporation gas can branch on the driving fluid supply line L2 to connect the power generation engine 32 and supply the liquefied gas vaporized by the vaporizer 23 to the power generation engine 32 .

The evaporation gas suction line L4 connects the liquefied gas storage tank 20 and the evaporation gas suction unit 41 so that the evaporation gas generated in the liquefied gas storage tank 10 is supplied to the evaporation gas suction unit 41 It can be sucked.

The evaporation gas supply line L5 connects the evaporation gas suction unit 41 and the refueling device 51 and supplies the mixed fluid discharged from the evaporation gas suction unit 41 to the refueling device 51 .

The first return line L6 connects the liquid remover 51 and the gas-liquid separator 60 and can supply the liquid-liquid mixture re-liquefied in the liquid remover 51 to the gas-liquid separator 60.

The second return line L7 connects the gas-liquid separator 60 and the liquefied gas storage tank 20 and is capable of recovering the liquid phase separated by the gas-liquid separator 60 to the liquefied gas storage tank 20.

Hereinafter, the individual configurations that are organically formed by the above-described respective lines (L1 to L7) to implement the gas processing system 1 will be described.

The liquefied gas storage tank 20 stores a liquefied gas or an evaporated gas to be supplied to the propulsion engine 31. The liquefied gas storage tank 20 must store the liquefied gas in a liquid state, at which time the liquefied gas storage tank 20 may have the form of a pressure tank.

In this embodiment, the evaporation gas generated due to the evaporation of the liquefied gas in the liquefied gas storage tank 20 is extracted through the evaporation gas suction unit 41 to be described later, whereby the evaporation gas can be efficiently managed.

Here, the type of the liquefied gas storage tank 20 is not particularly limited to various types such as a membrane-type tank or an independent tank, for example.

The boosting pump 21 can first pressurize the liquefied gas stored in the liquefied gas storage tank 20 and supply the liquefied gas to the high-pressure pump 22, which will be described later. Specifically, the boosting pump 21 is provided between the liquefied gas storage tank 20 and the high-pressure pump 22 on the liquefied gas supply line L1, and supplies the liquefied gas stored in the liquefied gas storage tank 20 to the high- It is possible to supply the pump 22 with a sufficient amount to prevent cavitation of the high-pressure pump 22.

The boosting pump 21 can extract the liquefied gas from the liquefied gas storage tank 20 and pressurize it to several to several tens of bars and the liquefied gas through the boosting pump 21 can be pressurized to 1 to 25 bar.

The liquefied gas stored in the liquefied gas storage tank 20 is in a liquid state. At this time, the boosting pump 21 may pressurize the liquefied gas discharged from the liquefied gas storage tank 20 to slightly increase the pressure and the temperature, and the liquefied gas pressurized by the boosting pump 21 may still be in a liquid state.

In the present embodiment, the boosting pump 21 can supply the maximum flow rate to the high-pressure pump 22. [ The maximum flow rate refers to the flow rate at which the booster pump 21 can discharge the maximum amount. In this case, since the liquefied gas in an amount larger than the required flow rate of the high-pressure pump 22 is transmitted from the boosting pump 21 to the high-pressure pump 22, smooth driving of the high-pressure pump 22 becomes possible.

The boosting pump 21 may be constructed in a disposition within the liquefied gas storage tank 20 or may be constructed in a centrifugal manner outside a position lower than the level of the liquefied gas stored in the liquefied gas storage tank 20 .

The high-pressure pump 22 can pressurize the liquefied gas supplied from the boosting pump 21 (pressurize at a high pressure of about 200 bar to 400 bar) to the vaporizer 23 to be described later. Specifically, the high-pressure pump 22 is provided between the booster pump 21 and the vaporizer 23 on the liquefied gas supply line L1, and is pressurized to a pressure of about 6 to 8 bar To the vaporizer 23 by secondary pressurization to a high pressure of about 200 to 400 bar.

The high pressure pump 22 can supply the pressure required by the propulsion engine 31 by pressurizing the high pressure pump 22 at a high pressure of about 200 to 400 bar and supplying it to the propulsion engine 31 via the vaporizer 23, (Not shown) to generate thrust through the liquefied gas.

The high-pressure pump 22 pressurizes the liquid-state liquefied gas discharged from the boosting pump 21 to a high pressure, and changes the phase of the liquefied gas to a supercritical state having a temperature and a pressure higher than the critical point . At this time, the temperature of the liquefied gas in the supercritical state may be minus 20 degrees or less, which is relatively higher than the critical temperature.

Alternatively, the high-pressure pump 22 can pressurize the liquefied gas in the liquid state to a super-cooled liquid state by pressurizing it at a high pressure. Here, the liquefied gas in the subcooled liquid state is a state in which the pressure of the liquefied gas is higher than the critical pressure and the temperature is lower than the critical temperature.

Specifically, the high-pressure pump 22 pressurizes the liquid-state liquefied gas discharged from the boosting pump 21 to a high pressure of 200 to 400 bar, while allowing the temperature of the liquefied gas to be lower than the critical temperature, Phase state to a subcooled liquid state. Here, the temperature of the liquefied gas in the subcooled liquid state may be minus 140 degrees to minus 60 degrees lower than the critical temperature.

In the embodiment of the present invention, when the high-pressure pump 22 is provided in parallel and one of the high-pressure pumps 22 malfunctions or shut down, the other high-pressure pump 22 can operate So that the liquefied gas supplied from the boosting pump 21 can be reliably and stably supplied to the propulsion engine 31.

The vaporizer 23 is provided on the liquefied gas supply line L 1 and can heat the high-pressure liquefied gas discharged from the high-pressure pump 22. Specifically, the vaporizer 23 is provided on the liquefied gas supply line L1 between the propulsion engine 31 and the high-pressure pump 22, and heats the high-pressure liquefied gas supplied from the high-pressure pump 22, 31 can be supplied in a desired state.

That is, the vaporizer 23 heats the liquefied gas in the subcooled liquid state or the supercritical state while maintaining the pressure of 200 bar to 400 bar, which is the pressure discharged from the high-pressure pump 22, And can supply it to the propulsion engine 31 after conversion.

At this time, the vaporizer 23 can use Glycol Water, Sea Water, Steam, or engine exhaust gas as a fuel for heating the liquefied gas, and the pressure of the liquefied gas at a high pressure And can be supplied to the propulsion engine 31 without any change.

The propulsion engine 31 generates the propulsion power of the ship (not shown) using the liquefied gas stored in the liquefied gas storage tank 20 or the evaporative gas generated in the liquefied gas storage tank 20 as fuel.

The propulsion engine 31 requires a liquefied gas or an evaporation gas, and can be driven using the raw material as the raw material. Propulsion engine 31 may be, but is not limited to, a MEGI engine as a high pressure gas injection engine.

Here, the propulsion engine 31 may be connected to the liquefied gas storage tank 20 through the liquefied gas supply line L1, and may be supplied with the liquefied gas or the evaporated gas pressurized at a high pressure of about 200 to 400 bar.

The propulsion engine 31 may be a pressurized or evaporated gas or liquefied gas through the high pressure pump 22 and the vaporizer 23 and may be a high pressure engine using a high pressure vapor of about 300 bar, An engine for rotating the propeller shaft S directly to drive the propeller shaft P, or an engine for generating other power.

As the piston (not shown) inside the cylinder (not shown) reciprocates by the combustion of the liquefied gas or the evaporative gas, the engine rotates the crankshaft (not shown) connected to the piston and is connected to the crankshaft A shaft (not shown) can be rotated. Accordingly, as the propeller P connected to the propeller shaft S rotates when the propulsion engine 31 is driven, the ship can move forward or backward.

Of course, in this embodiment, the propulsion engine 31 may be an engine for driving the propeller P, but may be an engine for generating power or an engine for generating other power. That is, the present embodiment does not specifically limit the kind of high-pressure consumer 91. [ However, the high-pressure consumer 61 may be an internal combustion engine that generates a driving force by combustion of evaporative gas, liquefied gas, flash gas and oil.

The propulsion engine 31 may be a DF engine in which a heterogeneous fuel can be used. A heterogeneous fuel engine is a two-stroke DF engine, usually driven by a diesel cycle. In this diesel cycle, air is compressed by the piston, the compressed high-temperature air is ignited by a pilot fuel, and the remaining high-pressure gas is injected and exploded.

In this case, HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil) is used as the ignition fuel, and the ratio of the ignition fuel to the high-pressure gas is about 5:95, and the injection amount of the ignition fuel can be adjusted from 5 to 100% Do. Therefore, the ignition fuel is also usable as the driving fuel for the engine.

That is, when the injection amount of the ignition fuel is about 5%, evaporative gas (or heated liquefied gas; about 95%) is mainly used as the engine driving fuel, and when the injection amount of the ignition fuel is 100% Fuel (oil) is all used.

At this time, when the injection amount of the ignition fuel is about 50% (and about 50% of the evaporation gas), the ignition fuel and the evaporation gas are mixed and not ignited into the engine, but the ignition fuel is ignited first to generate a calorific value, Gas is introduced and exploded to produce a calorific value, thereby producing a calorific value required for driving the engine.

Further, the propulsion engine 31 may be a low-speed two-stroke low-pressure gas injection engine (XDF). The propulsion engine 31 may be connected to the liquefied gas storage tank 20 through the liquefied gas supply line L1 and may be supplied with the liquefied gas or the evaporated gas pressurized at a low pressure of about 25 to 40 bar , The high pressure pump 22 may be omitted, unlike the case where the propulsion engine 31 is a MEGI engine). The propulsion engine 31 is a device for propelling the evaporation gas or liquefied gas, which has been pressurized and heated through the boosting pump 21 and the vaporizer 23, Pressure engine that uses a low-pressure evaporation gas of about 40 bar and is capable of rotating the propeller shaft S directly in order to drive the propeller P, Or may be an engine for generating other power.

The low-speed two-stroke low-pressure gas injection engine in the embodiment of the present invention may be a 2s DF engine (XDF engine) developed by wartsila, and may be driven according to an Otto cycle.

That is, in the low-speed two-stroke low-pressure gas injection engine, the air-fuel mixture supplied to the cylinder is first compressed to the top dead center, and at the moment when ignition is performed by the pilot fuel from the outside at the compression top dead center, So that explosive power is generated. At this time, the air-fuel mixture mass ratio may be in the form of a Lean burn engine which may be in a lean state less than 14.7: 1.

In this case, HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil) is used as the ignition fuel, and the ratio of the ignition fuel to the high-pressure gas is about 1:99.

The low-speed two-stroke low-pressure gas injection engine can generate power by supplying the liquefied gas from 25 to 40 bar, and the state of the supplied ethane can be changed depending on the state required by the low-speed two-stroke low-pressure gas injection engine.

The MEGI engine requires a high pressure of about 200 bar to about 300 bar and a power consumption of about 210 KW to about 220 KW (about 215 KW) The low pressure gas injection engine has the effect of reducing the power consumption by about 13 KW to about 17 KW (about 15 KW) for driving at a low pressure of 25 to 40 bar, have.

In addition, the MEGI engine has a disadvantage in that the driving pressure is so high that the gas processing system that accompanies it is very complicated and takes up a lot of space in order to generate the pressure required by the MEGI engine. On the other hand, the low-speed two-stroke low-pressure gas injection engine is advantageous in that the fuel supply system is very simple and the space occupied by the low-pressure gas injection engine is low because the driving pressure is low.

The power generation engine 32 may be, for example, a DFDE engine as a consumer using low-pressure evaporation gas of about 6 to 10 bar. The power generation engine 32 is a heterogeneous fuel engine that can use a different kind of fuel and can use not only evaporation gas but also oil as fuel. However, the evaporation gas and oil are not mixed and supplied, and the evaporation gas or oil is selectively supplied . This is to prevent the mixture of two materials having different combustion temperatures from being mixed, thereby preventing the efficiency of the power generation engine 32 from deteriorating.

Here, the power generation engine 32 can be driven by receiving the evaporation gas supplied from the evaporation gas suction unit 41. The power generation engine 32 may be a generator (e.g., DFDG), a boiler (for example, a boiler that generates steam) as well as the DFDE engine described above that requires evaporative gas and can be driven with the raw material , But is not limited thereto.

The power generation engine 32 is supplied with the evaporation gas supplied from the evaporation gas suction unit 41 and can be driven to generate electric power and supply the generated electric power to the refueling device 51.

At this time, the power generation engine 32 is connected to the remelting device 51 by a power supply line (not shown) to supply the power generated by the power generation engine 32, A converter (not shown) is provided to convert the electric power generated by the power generation engine 32 into electric power required by the refueling device 51.

The evaporation gas sucking unit 41 supplies the vaporized liquid liquefied gas heated by the vaporizer 23 through the high pressure pump 22 to the driving fluid supply line L2 from the vaporizer 23, And the evaporation gas generated in the liquefied gas storage tank 20 may be sucked through the evaporation gas suction line L4 and then supplied to the re-liquefier 51. [0050] Here, the evaporation gas sucking unit 41 may be an ejector, an electric actuator, or a jet pump.

Specifically, the evaporation gas suction unit 41 is connected to the driving fluid supply line L2, the evaporation gas suction line L4, and the evaporation gas supply line L5, And is supplied with the liquefied gas and can suck the evaporated gas generated in the liquefied gas storage tank 20 through the evaporated gas suction line L4 and supply the evaporated gas to the liquefaction device 51. [

Here, the evaporation gas sucking unit 41 can only supply the mixed fluid (evaporation gas) to be discharged to the refueling device 51 without supplying it to the power generation engine 32.

The power generation engine 32 can be driven only when it is supplied with fuel (evaporation gas or liquefied gas) having a pressure of approximately 6 to 10 bar. However, even if the evaporation gas suction unit 41 substantially increases the pressure by sucking the evaporation gas of 1 to 1.06 bar generated in the liquefied gas storage tank 20, the pressure rise of from 6 to 10 bar can be suppressed in the present technology It is near impossible. Therefore, the present technology has a disadvantage in that a separate pressurizing device is additionally provided to be supplied to the power generation engine 32 so that the design cost is increased to be supplied to the evaporation gas suction unit 41. Therefore, in the embodiment of the present invention, the evaporation gas sucking unit 41 can supply the mixed fluid (evaporation gas) to be discharged only to the refueling device 51 without supplying it to the power generation engine 32.

The re-liquefier 51 can be easily driven even at a low pressure because the range of pressure that can be driven is wide compared to the power generation engine 32 and the operating pressure is only 3 to 5 bar. Therefore, in the embodiment of the present invention, the discharge fluid of the evaporation gas suction unit 41 can be optimally used by supplying the low-pressure mixed fluid discharged from the evaporation gas suction unit 41 only to the re-liquefier 51 , The design cost can be reduced accordingly, and the system drive reliability can be improved.

The evaporation gas sucking unit 41 can calculate a driving fluid amount for sucking a certain amount of evaporation gas to suck a certain amount of evaporation gas generated in the liquefied gas storage tank 20, And can be supplied through the driving fluid supply line L2.

The evaporation gas sucking unit 41 receives the gaseous liquefied gas by the driving fluid and sucks the evaporated gas generated in the liquefied gas storage tank 20 to mix with the gaseous liquefied gas as the driving fluid, The kinetic energy is converted into the kinetic energy of the entire mixed fluid and then the velocity of the mixed fluid at the end portion where the end face of the nozzle (not shown) of the vapor gas sucking unit 41 is enlarged decreases, The kinetic energy is again converted into pressure. As a result, the evaporation gas of 1 to 1.06 bar generated in the liquefied gas storage tank 20 obtains a pressure of about 3 to 5 bar (preferably about 4 bar).

In the present invention, the driving fluid after the pressure of the liquefied gas supplied from the vaporizer 23 is introduced into the evaporation gas suction unit 41 at a pressure of about 200 to 400 bar (preferably about 300 bar) or the like, (Preferably about 4 bar) by supplying a pressure transferring capacity, which is a driving fluid flow rate, to the suction fluid (evaporation gas generated in the liquefied gas storage tank 10) by a pressure of about 3 to 5 bar .

Here, since the pressure of the driving fluid is high, the pressure of the suction fluid can be easily raised even with a small amount of fluid.

In the embodiment of the present invention, the evaporation gas suction unit 41 can independently supply the mixed fluid to the remelting device 51 at a constant flow rate regardless of the speed at which the ship is propelled. In this case, the speed at which the ship is propelled can be controlled by supplying the liquefied gas stored in the liquefied gas storage tank 20 to the propulsion engine 31 through the boosting pump 21 and the high-pressure pump 22. That is, the boosting pump 21 and the high-pressure pump 22 are driven depending on the propulsion speed of the ship, and the evaporation gas suction unit 41 can be driven independently of the propulsion speed of the ship.

Accordingly, the processing of the evaporated gas generated in the liquefied gas storage tank 20 can be continuously performed, and the internal pressure of the liquefied gas storage tank 20 can be effectively managed.

The remelting device 51 may be connected to the evaporation gas suction unit 41 through the evaporation gas supply line L5 and may be connected to the gas-liquid separator 60 through the first return line L6. In this case, one liquid remover 51 may be provided, and a plurality of liquid removers 51 may be provided corresponding to the number of the evaporation gas suction units 41. [

The liquefaction device 51 can return the mixed fluid discharged from the evaporation gas suction unit 41 to the liquefied gas storage tank 20 by re-liquefying the entire amount of the fluid (the fluid in which the evaporation gas and the liquid liquefied gas are mixed) .

The re-liquefied refrigerant is an inert gas, preferably nitrogen (N2).

The re-liquefier 51 includes a re-liquefying heat exchanger (not shown), a re-liquefying inflator (not shown), a re-liquefying compressor (not shown) and a re-liquefaction circulation line (not shown) The liquefied circulation line is provided with a re-liquefied heat exchanger, a re-liquefied expander, and a re-liquefied compressor, so that the re-liquefied refrigerant circulates the respective units in the order of the re-liquefied compressor, the re-liquefied expander and the re-liquefied heat exchanger.

Specifically, the re-liquefied refrigerant is heated by receiving a heat source from the mixed gas in the re-liquefying heat exchanger, passed through the re-liquefying heat exchanger, and then supplied to the re-liquefied compressor. The re-liquefied refrigerant is multi-stage pressurized in the re-liquefied compressor, the pressure is raised, and the re-liquefied heat exchanger is again supplied to the re-liquefier. The re-liquefied refrigerant is expanded in the re-liquefied inflator, the pressure is lowered, and thereby the temperature is lowered, thereby obtaining the cold source. The re-liquefied refrigerant obtained through this process is supplied to the re-liquefying heat exchanger again, and is heat-exchanged with the mixed gas at room temperature to cool the mixed gas, thereby re-liquefying the mixed gas. The re-liquefied refrigerant in which the mixed gas is re-liquefied obtains the heat source in the opposite charge portion and is supplied to the re-liquefied compressor again so that the above-described process is repeatedly circulated.

The heat exchange cycle of the remanufacturing device 51 described above may be a reversed cycle cycle, but the re-liquefying device 51 applied to the embodiment of the present invention is not limited thereto, and may be a vapor compression refrigeration cycle using mixed refrigerant and pure refrigerant Cascade method) and other refrigeration cycles (eg, Claude refrigerator (expansion turbine and expansion valve can be used in parallel)) can also be applied.

As described above, the re-liquefier 51 has many equipment used to re-liquefy the evaporated gas and consumes much more power than the other equipment.

Therefore, in the embodiment of the present invention, electric power can be supplied from the shaft generator 71 that reproduces surplus power with electric power in order to additionally reinforce electric power to the remapping device 51, or consumes surplus evaporation gas So that power can be supplied from the power generation engine 32 that reproduces the power.

As a result, in the embodiment of the present invention, the power used in the liquefaction device 51 can be sufficiently supplied, driving reliability can be improved, and the processing of the evaporation gas can be performed very efficiently.

The gas-liquid separator 60 may be connected to the liquefaction device 51 via the first return line L6 and may be connected to the liquefied gas storage tank 20 through the second return line L7.

The gas-liquid separator 60 is capable of separating the mixed liquid that has been re-liquefied through the first return line L6 from the liquefaction device 51 into a gas phase and a liquid phase, and the separated liquid phase passes through the second return line L7 To the liquefied gas storage tank 20 through the opening of the liquefied gas storage tank 20.

The shaft generator 71 is operatively associated with the propeller shaft S to generate power from at least part of the power from the propulsion engine 31 and to supply power to the refueling device 51 . Or shaft generator 71 may supply power to an energy storage system (not shown) to store the power in the form of energy.

The shaft generator 71 provides resistance to the drive of the propulsion engine 31 where the propulsion engine 31 is a MEGI engine which allows the ship to increase the output of the propulsion engine 31, The liquefied gas or the evaporated gas can be consumed without increasing the speed.

The shaft generator 71 is connected to a remelting device 51 by a power supply line (not shown) to supply electric power generated by the shaft generator 71, and a converter (Not shown) can be provided to convert the electric power generated in the shaft generator 71 into electric power required by the refueling device 51. [

Thus, the gas treatment system 1 according to the present invention and the vessel containing it effectively supply the liquefied gas and / or the evaporated gas from the liquefied gas storage tank 20 to the customers 31 and 51, .

2 is a conceptual diagram of a gas processing system according to a second embodiment of the present invention.

2, the gas processing system 2 according to the second embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, a forced vaporizer 401, evaporation gas sucking units 42a, 42b and 42c, res liquefaction units 52a, 52b and 52c, a gas-liquid separator 60 and a first control unit 81 .

The structure of the forced vaporizer 401 and the first control unit 81 is added to the present embodiment and the constitution of the power generation engine 32 and the shaft generator 71 is omitted and the evaporation gas suction units 42a, And the liquid removers 52a, 52b and 52c are arranged in parallel, and the other structures are the same as or similar to those of the first embodiment. The same or corresponding elements as those of the first embodiment described above are denoted by the same reference numerals, and redundant description thereof will be omitted.

Hereinafter, the gas processing system 2 according to the second embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, it may further include a driving fluid supply line L8.

The driving fluid supply line L8 is branched between the boosting pump 21 and the high-pressure pump 22 on the liquefied gas supply line L1 to connect the evaporation gas intake units 42a, 42b and 42c, (401).

The driving fluid supply line L8 supplies the liquefied gas pressurized at a low pressure by the booster pump 21 to the forced vaporizer 401 and supplies the liquefied gas forcedly vaporized in the forced vaporizer 401 to the evaporation gas sucking unit 42a 42b, and 42c to be used as the driving fluid for the evaporation gas suction units 42a, 42b, and 42c. That is, the drive fluid supply line L8 includes a first drive fluid supply line L8a connected to the evaporation gas intake unit 42a, a second drive fluid supply line L8b connected to the evaporation gas intake unit 42b, And a third drive fluid supply line L8c connected to the evaporation gas suction unit 42c.

The first control valve V1 and the second control valve V2 are provided in the driving fluid supply line L8 so that the supply amount of the vaporized liquefied gas can be controlled according to the opening degree of the valve, And can be controlled by a wired or wireless connection.

Specifically, the first control valve V1 is provided on the first drive fluid supply line L8a and controls the flow rate of the vaporized liquefied gas flowing on the first drive fluid supply line L8a through the opening adjustment And the second control valve V2 is provided on the second drive fluid supply line L8b and is capable of controlling the flow rate of the vaporized liquefied gas flowing on the second drive fluid supply line L8b The flow rate can be controlled. Here, the second control valve V2 is also provided on the third drive fluid supply line L8c, and is formed as a three-way valve so that the vaporized liquefied gas flowing on the third drive fluid supply line L8c, The flow rate of the gas can be controlled.

Further, a separate pressure reducing device may not be provided on the driving fluid supply line L8.

In the embodiment of the present invention, a plurality of evaporation gas suction units 42a, 42b, and 42c may be provided and may be provided in parallel on the driving fluid supply line L8.

The evaporation gas sucking units 42a, 42b and 42c may be connected to the evaporation gas suction line L4 in parallel and connected to the re-liquefying units 52a and 52b through evaporation gas supply lines L5a, L5b and L5c, , 52c.

The forced vaporizer (401) forcibly vaporizes the liquefied gas stored in the liquefied gas storage tank (20).

Specifically, the forced vaporizer 401 is provided upstream of the evaporative gas suction units 42a, 42b, and 42c on the driving fluid supply line L8 and supplies the liquefied gas stored in the liquefied gas storage tank 10 to the booster pump 21 to supply the amount of drive fluid necessary for the evaporation gas suction units 42a, 42b, 42c.

The forced vaporizer 401 is a heat source for vaporizing the liquefied gas or exhaust gas discharged from the lubricating oil used in the propulsion engine 31 or the power generation engine 32, the propulsion engine 31 or the power generation engine 32, Liquefied refrigerant heated in the liquefaction device 51 can be used.

The first control unit 81 regulates the amount of vaporized liquefied gas to be supplied to each of the evaporation gas suction units 42a, 42b, and 42c.

Specifically, the first control unit 81 controls the supply amount of the vaporized liquefied gas to each of the evaporation gas suction units 42a, 42b, and 42c provided in parallel so that the evaporation gas suction units 42a, 42b, and 42c The amount of evaporative gas sucked from the liquefied gas storage tank 20 can be controlled.

The first control unit 81 controls the degree of opening of the first and second control valves V1 and V2 so that the evaporation gas intake units 42a, 42b, and 42c are evaporated from the liquefied gas storage tank 20, It is possible to control the amount of gas sucked.

The first control unit 81 can be connected to the detection sensor 81a to be described later by wire or wirelessly and can receive the internal pressure information of the liquefied gas storage tank 20.

Specifically, when the internal pressure measured by the detection sensor 81a is equal to or higher than the predetermined pressure, the first control unit 81 controls the first and second control valves V1 and V2 to sequentially open the openings And when the internal pressure measured by the detection sensor 81a is lower than the preset pressure, the opening degree of the first and second control valves V1 and V2 may be sequentially decreased.

That is, the first control unit 81 intermittently controls the amount of the evaporative gas sucked in the liquefied gas storage tank 20 without a separate decompressor, by connecting the plurality of parallelly connected evaporative gas suction units 42a, 42b, and 42c .

The detection sensor 81a can measure the internal pressure of the liquefied gas storage tank 20. Specifically, the detection sensor 81a is formed on the inside or outside of the liquefied gas storage tank 20 to measure the internal pressure of the liquefied gas storage tank 20, and the first control unit 81 and the wired or wireless So that the internal pressure information of the liquefied gas storage tank 20 can be transmitted.

In the case where only one evaporation gas suction unit exists, the pressure of the driving fluid supplied to the evaporation gas suction unit must be adjusted in order to control the amount of evaporation gas that is generated in the liquefied gas storage tank 20, A separate decompression device must always be provided on the driving fluid supply line L8.

In order to solve this problem, in the embodiment of the present invention, a plurality of evaporation gas sucking units 42a, 42b, 42c are provided in parallel so that the amount of the evaporating gas sucked in the liquefied gas storage tank 20 can be efficiently Can be controlled.

Therefore, in the embodiment of the present invention, it is possible to reduce the construction cost of the system, and to effectively treat the evaporated gas generated in the liquefied gas storage tank 20.

Thus, the gas treatment system 2 according to the present invention and the vessel containing it effectively supply the liquefied gas and / or the evaporated gas from the liquefied gas storage tank 20 to the customers 31 and 51, .

3 is a conceptual diagram of a gas processing system according to a third embodiment of the present invention.

3, the gas processing system 3 according to the third embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, a forced vaporizer 401, evaporation gas sucking units 42a, 42b and 42c, res liquefaction units 52a, 52b and 52c, a gas-liquid separator 60 and a first control unit 81 .

In this embodiment, the driving fluid supply line L8 is changed to the driving fluid supply line L2, and the other configurations are the same as or similar to those of the second embodiment. The same or corresponding elements as those of the second embodiment described above are denoted by the same reference numerals and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 3 according to a third embodiment of the present invention will be described with reference to FIG.

2) is provided between the boosting pump 21 and the high-pressure pump 22 in the second embodiment of the present invention, in the third embodiment of the present invention, unlike the case where the driving fluid supply line L8 A line L2 may be provided on the carburetor 23 and the propulsion engine 31. [

The driving fluid supply line L2 includes a first driving fluid supply line L2a connected to the evaporation gas suction unit 42a, a second driving fluid supply line L2b connected to the evaporation gas suction unit 42b, And a third drive fluid supply line L2c connected to the evaporation gas suction unit 42c and the first control valve V1 is provided on the first drive fluid supply line L2a, The second control valve V2 may be provided on the second drive fluid supply line L2b and the second control valve V2 may be provided on the second drive fluid supply line L2b by controlling the flow rate of the vaporized liquefied gas flowing on the first drive fluid supply line L2a , It is possible to control the flow rate of the vaporized liquefied gas flowing on the second driving fluid supply line (L2b) through opening regulation.

Here, the second control valve V2 is also provided on the third drive fluid supply line L2c, and is formed as a three-way valve so that the vaporized liquefied gas flowing on the third drive fluid supply line L2c, The flow rate of the gas can be controlled.

In this case, the driving fluid supply line L2 may not have a separate pressure reducing device.

As a result, in the third embodiment of the present invention, compared to the second embodiment of the present invention, the forced vaporizer 401 can be omitted, and it is not necessary to provide a separate decompression device, , 42b, and 42c of the liquefied gas storage tank 20 can be controlled by controlling the flow rate of the evaporative gas sucked in the liquefied gas storage tank 20, thereby reducing the system construction cost.

4 is a conceptual diagram of a gas processing system according to a fourth embodiment of the present invention.

4, the gas processing system 4 according to the fourth embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, a power generation engine 32, a buffer tank 402, evaporation gas intake units 43a and 43b, a refueling unit 51, a gas-liquid separator 60, and a second control unit 82 .

In the present embodiment, the buffer tank 402, the second control unit 82 and the evaporation gas suction line L9 are added, the first control unit 81 is omitted, and the other configurations are the same as the first to third implementations The same as or similar to the example. The same or corresponding elements as those of the first to third embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 4 according to a fourth embodiment of the present invention will be described with reference to FIG.

In the fourth embodiment of the present invention, the evaporation gas suction units 43a and 43b may be connected to each other in series.

Here, the driving fluid supply line L2 includes a first driving fluid supply line L2 branched on the liquefied gas supply line L1 and connected to the evaporation gas suction unit 43a, a first driving fluid supply line L2, And the evaporation gas suction line L4 may be formed as a first evaporation gas suction line L4 and a second driving fluid supply line L2a branched to the evaporation gas suction unit 43b, The suction line L9 may be referred to as a second evaporation gas suction line L9.

Specifically, the evaporation gas suction units 43a and 43b supply vaporized liquefied gas from the first driving fluid supply line L2 to the evaporation gas generated in the liquefied gas storage tank 20 through the evaporation gas suction line L4 A first evaporation gas suction unit 43a which is sucked through the first evaporation gas suction unit 43a and a second evaporation gas suction unit 43b which is supplied with the liquefied gas vaporized from the second drive fluid supply line L2a, And a second evaporation gas suction unit 43b sucked through the suction line L9.

The second evaporation gas sucking unit 43b sucks the mixed gas discharged from the first evaporating gas sucking unit 43a and further pressurizes the pressurized mixed fluid to the re-liquefier 51 or the power generating engine 32).

At this time, the first mixed fluid discharged from the first evaporation gas suction unit 43a has a first pressure (3 to 5 bar), and the second mixed fluid discharged from the second evaporation gas suction unit 43b has a first pressure And a second pressure (6 to 10 bar) higher than the pressure.

Accordingly, in the embodiment of the present invention, the power generation engine 32 can be driven by receiving the second mixed fluid pressurized through the second evaporative gas intake unit 43b without using a separate pump or a compressor.

In an embodiment of the present invention, the evaporation gas second branch line L10 may further be included.

The second branch line L10 of the evaporation gas is branched on the evaporation gas supply line L5 and connected to the power generation engine 32. The second pressure (6 to 10 bar) discharged from the second evaporation gas intake unit 43b, To the power generation engine (32).

The second control unit 82 can control whether the first and second evaporative gas suction units 43a and 43b are driven according to the fuel consumption amount of the propulsion engine 31. [ The second control unit 82 is connected to the propulsion engine 31 and the first and second evaporation gas intake units 43a and 43b either in a wired or wireless manner to receive the fuel consumption amount information of the propulsion engine 31, The driving signal can be transmitted to the first and second evaporation gas suction units 43a and 43b.

Specifically, when the fuel consumption amount of the propulsion engine 31 is equal to or higher than the predetermined consumption amount, the second control unit 82 drives only the first evaporation gas intake unit 43a, and only the first mixed fluid is supplied to the refueling device 51. [ The first and second evaporative gas suction units 43a and 43b are all driven so that the second mixed fluid is supplied to the power generation engine 32. In the case where the fuel consumption amount of the propulsion engine 31 is less than the predetermined consumption amount, As shown in Fig.

That is, in this embodiment, when the fuel consumption amount of the propulsion engine 31 is large, the amount of the drive fluid flowing into the first evaporation gas suction unit 43a is reduced, so that the second evaporation gas suction unit 43b stops driving, 1 evaporative gas sucking unit 43a only operates to supply the first mixed fluid discharged at 3 to 5 bar (preferably 4 bar) only to the refueling device 51. When the fuel consumption of the propulsion engine 31 is small, The first and second evaporative gas suction units 43a and 43b are all driven so that the amount of the driving fluid discharged from the first evaporation gas suction unit 43a is increased to 6 to 10 bar 2 mixed fluid to the power generation engine 32.

As described above, according to the fourth embodiment of the present invention, the evaporative gas can be selectively consumed in the refueling device 51 or the power generation engine 32 in accordance with the fuel consumption amount of the propulsion engine 31 through the second control section 82 And the efficiency of evaporation gas consumption is maximized.

The buffer tank 402 is provided on the second evaporation gas suction line L9 and is connected to the second drive fluid supply line L2a when the first and second evaporation gas suction units 43a and 43b are driven, It is possible to prevent the fluid supplied to the second evaporation gas suction unit 43b from flowing back to the first evaporation gas suction unit 43a.

That is, even if the fluid passing through the second evaporative gas suction unit 43b flows back to the first evaporative gas suction unit 43a, the buffer tank 402 temporarily stores the fluid to be backflowed so that the pressure is lost, And the safety of the liquefied gas storage tank 20 is increased.

As described above, in the fourth embodiment of the present invention, a plurality of the evaporation gas suction units 43a and 43b are arranged in series to supply the discharge fluid of the evaporation gas suction units 43a and 43b to the power generation engine 32 ) Can be consumed.

Therefore, in the embodiment of the present invention, the system construction cost is reduced and the evaporation gas suction units 43a and 43b are used instead of the complicated drive devices such as a pump and a compressor, .

5 is a conceptual diagram of a gas processing system according to a fifth embodiment of the present invention.

5, the gas processing system 5 according to the fifth embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, A gas-liquid separator 60, and a third control unit 83. The propulsion engine 31, the power generation engine 32, the evaporation gas suction unit 44, the re-liquefier 51,

This embodiment is different from the first embodiment in that the connection line supplied to the power generation engine 32 in the first embodiment is changed from the evaporated gas first branch line L3 to the evaporated gas second branch line L10, And other configurations are the same as or similar to those of the first to fourth embodiments. The same or corresponding elements as those of the first to fourth embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 5 according to a fifth embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, the flow rate control valve B1 and the supply control valve B2 may be additionally provided. The flow control valve B1 and the supply control valve B2 may be connected to the third control unit 83 to be described later by wire or wirelessly and receive the opening control driving instruction from the third control unit 83. [

The first flow control valve B1 is provided on the evaporation gas supply line L5 and controls the flow rate of the evaporation gas flowing on the evaporation gas supply line L5 according to the drive information transmitted from the third control unit 83 Can be controlled.

 The supply control valve B2 is provided at a position where the second branch line L10 of the evaporation gas is branched on the evaporation gas supply line L5 and is supplied to the evaporation gas supply line L5 according to the drive information transmitted from the third control unit 83. [ It is possible to control whether the flow direction of the evaporation gas flowing on the line L5 is supplied to the power generation engine 32 or the refueling device 51. [

The third control section 83 controls the flow rate of the mixed fluid flowing on the evaporation gas supply line L5 to control the flow rate of the evaporation gas flowing on the evaporation gas suction line L4. The third control unit 83 is connected to the flow rate regulating first valve B1 and the supply control valve B2 either in a wired or wireless manner and is capable of transmitting an opening regulation driving command, And can receive the internal pressure information of the liquefied gas storage tank 20.

Specifically, the third control section 83 receives the internal pressure information of the liquefied gas storage tank 20 from the detection sensor 81a and can control the flow rate regulating first valve B1. More specifically, 3 control unit 83 increases the opening degree of the first flow control valve B1 when the internal pressure of the liquefied gas storage tank 20 is equal to or higher than the predetermined pressure so that the evaporation gas generated in the liquefied gas storage tank 20 flows into the evaporation gas And the amount of the refrigerant flowing into the liquefied gas storage tank 20 is reduced by reducing the opening degree of the first flow control valve B1 when the internal pressure of the liquefied gas storage tank 20 is lower than the predetermined pressure. So that the amount of the evaporated gas generated in the evaporation gas suction line L4 is reduced.

The third control unit 83 can receive the internal pressure information of the liquefied gas storage tank 20 from the detection sensor 81a and can control the supply control valve B2. More specifically, the third control unit 83 83 closes the opening of the supply control valve B2 in the direction of the liquefaction device 51 when the internal pressure of the liquefied gas storage tank 20 is equal to or higher than the preset pressure, When the internal pressure of the liquefied gas storage tank 20 is lower than the predetermined pressure, the opening of the supply control valve B2 in the direction of the power generation engine 32 is closed to supply the evaporated gas It is possible to control so that the mixed fluid discharged from the suction unit 44 is supplied only to the remelting device 51. [ Of course, in this case, the mixed fluid supplied to the power generation engine 32 may be pressurized to 6 to 10 bar (preferably 6.5 bar) by a separate pressurizing device.

As described above, in the fifth embodiment of the present invention, the flow rate or pressure of the mixed fluid discharged from the evaporation gas suction unit 44 is controlled without adjusting the flow rate or pressure of the evaporation gas sucked by the evaporation gas suction unit 44 So that the suction amount of the evaporated gas sucked in the liquefied gas storage tank 20 can be controlled.

Therefore, in the fifth embodiment of the present invention, it is possible to control the suction amount of the evaporated gas sucked in the liquefied gas storage tank 20 even without an additional decompression device or valve on the evaporated gas suction line L4, It is possible to effectively treat the evaporated gas.

6 is a conceptual diagram of a gas processing system according to a sixth embodiment of the present invention.

6, the gas processing system 6 according to the sixth embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, A gas-liquid separator 60 and a fourth control unit 84. The propulsion engine 31, the power generation engine 32, the evaporation gas intake unit 45, the refueling unit 51,

In the fifth embodiment, in the fifth embodiment, the third control section 83 is changed to the fourth control section 84, and the flow rate regulating second valve B3 ), And the other structures are the same as or similar to those of the first to fifth embodiments. The same or corresponding elements to those of the first to fifth embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, the gas processing system 6 according to the sixth embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, a second flow control valve B3 may be further provided. Here, the second valve B3 may be connected to the fourth control unit 84, which will be described later, by wire or wirelessly, and may receive the opening control driving instruction from the fourth control unit 84. [

The second flow control valve B3 is provided on the drive fluid supply line L2 and controls the flow rate of the evaporation gas flowing on the drive fluid supply line L2 according to the drive information transmitted from the fourth control unit 84 Can be controlled.

The fourth control unit 84 controls the flow rate of the vaporized liquefied gas flowing on the drive fluid supply line L2 to control the flow rate of the evaporated gas flowing on the vaporized gas suction line L4. Here, the fourth control unit 84 is connected to the flow rate control second valve B3 by wire or wireless, and can transmit the opening degree adjustment driving instruction. The fourth control unit 84 is connected to the detection sensor 81a by wire or wireless, And can receive the internal pressure information of the storage tank (20).

Specifically, the fourth control unit 83 receives the internal pressure information of the liquefied gas storage tank 20 from the detection sensor 81a and can control the flow rate control second valve B3. More specifically, 4 control unit 84 increases the opening degree of the second flow control valve B3 when the internal pressure of the liquefied gas storage tank 20 is equal to or higher than the preset pressure so that the evaporated gas generated in the liquefied gas storage tank 20 is discharged to the evaporation gas When the pressure in the liquefied gas storage tank 20 is lower than the predetermined pressure, the opening degree of the second flow control valve B3 is reduced to increase the flow rate of the liquefied gas in the liquefied gas storage tank 20, So that the amount of the evaporated gas generated in the evaporation gas suction line L4 is reduced.

As described above, in the sixth embodiment of the present invention, the flow rate or pressure of the drive fluid flowing into the evaporation gas suction unit 45 is controlled without adjusting the flow rate or pressure of the evaporation gas sucked in by the evaporation gas suction unit 45 So that the suction amount of the evaporated gas sucked in the liquefied gas storage tank 20 can be controlled.

Thus, in the sixth embodiment of the present invention, it is possible to control the suction amount of the evaporated gas sucked in the liquefied gas storage tank 20 even without an additional decompression device or valve on the evaporated gas suction line L4, It is possible to effectively treat the evaporated gas.

7 is a conceptual diagram of a gas processing system according to a seventh embodiment of the present invention.

7, the gas processing system 7 according to the seventh embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, evaporation gas suction units 46a and 46b, a remelting device 51, a gas-liquid separator 60 and a fifth control unit 85. [

In this embodiment, the fifth control unit 85, the first valve B4, and the second valve B5 are additionally provided in the third embodiment, and the other configurations are the same as those of the first to sixth embodiments . The same or corresponding elements as those of the first to sixth embodiments described above are denoted by the same reference numerals, and redundant description thereof will be omitted.

Hereinafter, a gas processing system 7 according to a seventh embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, a plurality of evaporation gas suction units 46a and 46b may be formed and connected in parallel. For example, the evaporation gas suction units 46a and 46b may be connected to the first evaporation gas suction unit 46a and the second evaporation gas suction unit 46a. And may be an evaporation gas sucking unit 46b.

The first evaporation gas sucking unit 46a may be a fixed capacity type or variable capacity type per hour for the evaporation gas suction processing amount and the evaporation gas suction processing amount may be fixed capacity type per hour . Here, the first evaporative gas suction unit 46a may be a variable ejector when the evaporative gas intake processing amount is variable capacity per hour, and may be connected to the fifth control unit 85, which will be described later, by wire or wireless, .

In the case where the first and second evaporation gas intake units 46a are of fixed capacity type per hour for the evaporation gas intake process amount and the evaporation gas intake processing amount is supplied from the driving fluid supply line L2 to the vaporized liquefied gas of 200 to 400 bar And when the first evaporation gas suction unit 46a is in the variable capacity type per hour, that is, when the first evaporation gas suction unit 46a is a variable type ejector, the evaporation gas suction throughput amount is 200 to 400 bar from the driving fluid supply line L2 Lt; RTI ID = 0.0 > kg / hr < / RTI >

In the embodiment of the present invention, the driving fluid supply line L2 is connected to the first driving fluid supply line L2a and the second evaporative gas suction unit 46b connected to the first evaporative gas suction unit 46a And the second evaporative gas suction line L4a connected to the first evaporative gas suction unit 46a and the second evaporative gas suction line L4a connected to the second evaporative gas suction unit 46a may be formed as a second driving fluid supply line L2b, And a second evaporation gas suction line L4b connected to the suction unit 46b.

Further, in the embodiment of the present invention, the first valve B4 and the second valve B5 may be additionally provided. Here, the first valve B4 and the second valve B5 may be connected to the fifth control unit 85 to be described later by wire or wirelessly, and may receive the drive instruction from the fifth control unit 85. [

The first valve B4 is provided on the first driving fluid supply line L2a and is connected to the first driving fluid supply line L2a in accordance with the driving information transmitted from the fifth control unit 85, The flow rate can be controlled. Here, the first valve B4 may be an on-off valve that intermittently turns on or off the opening degree, or may be an on-off valve that flows on the first driving fluid supply line L2a And may be a pressure reducing valve for reducing the vaporized liquefied gas.

The second valve B5 is provided on the second driving fluid supply line L2b and is connected to the second driving fluid supply line L2b in accordance with the driving information transmitted from the fifth control unit 85, The flow rate can be controlled. Here, the second valve B5 may be an on-off valve that intermittently turns on or off the opening degree.

The fifth control unit 85 can control the amount by which the first and second evaporative gas suction units 46a and 46b suck the evaporative gas according to the navigation state of the ship. Here, the fifth control unit 85 is connected to the first and second valves B4 and B5 by wire or wirelessly, and can transmit the opening adjustment driving instruction, and the first evaporation gas suction unit 46a and the wired or wireless communication unit And can transmit the suction capacity variable control instruction and can be connected to the detection sensor 81a by wire or wirelessly to receive the internal pressure information of the liquefied gas storage tank 20. [

When the first valve B4 and the second valve B5 are the first on-off valve B4 and the second on-off valve B5, which are both on-off valves, Off valve B4 and the second on-off valve B5 so that the first and second evaporative gas suction units 46a and 46b are opened and closed by the liquefied gas storage tank It is possible to control the amount by which the evaporation gas generated in the evaporator 20 is sucked.

Specifically, when the internal pressure measured by the detection sensor 81a is within the first preset pressure range, the fifth control unit 85 opens both the first and second on-off valves B4 and B5 Off valve B4 is ON when the internal pressure measured by the detection sensor 81a is within the second preset pressure range.

In this case, only the first evaporation gas sucking unit 46a processes only about 1500 kg / h, which is the amount of evaporation gas generated in the liquefied gas storage tank 20 during the balloon navigation, The first and second evaporating gas suction units 46a and 46b process the evaporation gas amount of about 3000 kg / h, so that the driving fluid of the evaporation gas suction units 46a and 46b need not be separately depressurized, 46a, and 46b can be intermittently controlled, thereby improving driving reliability and reducing the construction cost.

When the first valve B4 is the pressure reducing valve B4 and the second valve B5 is the on-off valve B5, the fifth control unit 85 controls the pressure reducing valve B4 and the on- (B5) to control the amount by which the first and second evaporation gas suction units (46a, 46b) suck the evaporative gas generated in the liquefied gas storage tank (20) according to the navigation state of the ship have.

Specifically, when the internal pressure measured by the detection sensor 81a is within the first predetermined pressure range, the fifth control unit 85 closes the opening of the on-off valve B5 and the pressure reducing valve B4 So that only the first evaporation gas suction unit 46a controls the evaporation gas generated in the liquefied gas storage tank 20 to be variably inhaled and the internal pressure measured by the detection sensor 81a is controlled to be the second preset pressure , The opening degree of the on-off valve B5 is opened and the second pressure control valve B4 is controlled so that the second evaporation gas suction unit 46b sucks the evaporation gas at a predetermined suction amount, 1 evaporation gas sucking unit 46a can suck in the evaporated gas at a variable suction amount.

The first evaporation gas sucking unit 46a can process only about 1000 kg / h to about 1700 kg / h of evaporation gas generated in the liquefied gas storage tank 20 during the balloon navigation, and the liquefied gas storage tank 20 The first and second evaporating gas suction units 46a and 46b process the evaporation gas amount of about 2500 kg / h to 3200 kg / h, It is possible to elastically apply the suction force of the evaporation gas suction units 46a and 46b to the suction ports of the evaporation gas suction units 46a and 46b without elastically depressurizing the driving fluid of the evaporation gas suction units 46a and 46b, The amount of the evaporation gas can be partially and partly controlled in a partly variable manner, thereby improving driving reliability and reducing the construction cost.

Further, in the embodiment of the present invention, when the first evaporation gas suction unit 46a is a variable ejector, the first valve B4 may be omitted, and only the second valve B5 may be connected to the on- As shown in FIG.

At this time, the fifth control unit 85 controls the first evaporation gas suction unit 46a and the on-off valve B5 so that the first and second evaporation gas suction units 46a and 46b ) Can absorb the amount of the evaporated gas generated in the liquefied gas storage tank (20).

Specifically, the fifth control unit 85 closes the opening of the on-off valve B5 when the internal pressure measured by the detection sensor 81a is within the first preset pressure range, Only the suction unit 46a controls the variable gas suction generated in the liquefied gas storage tank 20 to suck the variable and when the internal pressure measured by the detection sensor 81a is within the second preset pressure range, B5 is opened so that the second evaporation gas suction unit 46b sucks the evaporation gas at a predetermined suction amount while the first evaporation gas suction unit 46a sucks the evaporation gas at the variable suction amount can do.

In this way, only the second evaporative gas suction unit 46b processes only about 1500 kg / h, which is the amount of evaporative gas generated in the liquefied gas storage tank 20 at the time of collective voyage, and is generated in the liquefied gas storage tank 20 The first and second evaporating gas suction units 46a and 46b process the evaporation gas amount of about 3000 kg / h, and at the same time, the amount of the evaporation gas (2500 kg / h to 3200 kg / h) It is possible to partially and partially control the amount of evaporated gas in the evaporation gas suction units 46a and 46b without having to separately depressurize the driving fluid of the evaporation gas suction units 46a and 46b, The reliability is improved and the construction cost is reduced.

Here, the first preset pressure is the internal pressure formed by the evaporative gas generated in the liquefied gas storage tank 20 when the ship is a laden voyage, Voyage) is the internal pressure formed by the evaporation gas generated in the liquefied gas storage tank 20.

For example, the first preset pressure is an internal pressure formed when the amount of evaporation gas generated in the liquefied gas storage tank 20 is 1400 to 1600 kg / h, and the second predetermined pressure is generated in the liquefied gas storage tank 20 Which is formed when the evaporation gas amount is 2900 to 3100 kg / h.

As described above, the gas treatment system 7 according to the present invention and the vessel including the same effectively supply the liquefied gas and / or the evaporated gas from the liquefied gas storage tank 20 to the customers 31 and 51 to improve system stability and reliability Height is effective.

8 is a conceptual diagram of a gas processing system according to an eighth embodiment of the present invention.

8, the gas processing system 8 according to the eighth embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, A propulsion engine 31, an evaporation gas suction unit 47, a refueling device 51, and a gas-liquid separator 60.

In the present embodiment, the configuration of the vaporizer 23 in the first embodiment is changed, and the other configurations are the same as or similar to those of the first to seventh embodiments. The same or corresponding elements as those of the first to seventh embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 8 according to an eighth embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, the evaporator 23 is further supplied with the mixed fluid discharged from the evaporation gas suction unit 47 via the evaporation gas supply line L5, and is supplied to the evaporation gas suction unit 47 The mixed fluid to be discharged and the liquefied gas supplied from the high-pressure pump 22 are heat-exchanged, and the liquefied gas supplied from the high-pressure pump 22 can be vaporized.

Specifically, the vaporizer 23 can be provided between the evaporation gas suction unit 47 on the evaporation gas supply line L5 and the refueling device 51, and at the same time, the high pressure pump The vaporizer 23 can heat the liquefied gas supplied from the high pressure pump 22 and the mixed fluid supplied from the evaporation gas suction unit 47 through heat exchange between the liquefied gas supplied from the high pressure pump 22 and the propulsion engine 31 .

Here, the vaporizer 23 may be a precooler as viewed from the side of the liquefaction device 51.

In the embodiment of the present invention, it is not necessary to additionally provide a heat source to be supplied to the evaporator 23, thereby reducing the construction cost. In addition, the pre- so that the driving efficiency of the remelting device 51 can be increased.

Thus, the gas treatment system 8 according to the present invention and the vessel containing the same effectively supply liquefied gas and / or evaporated gas from the liquefied gas storage tank 20 to the customer 31, 51, thereby improving system stability and reliability Height is effective.

9 is a conceptual diagram of a gas processing system according to a ninth embodiment of the present invention.

9, the gas processing system 9 according to the ninth embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, a power generation engine 32, a variable frequency drive pump 403, a forced vaporizer 404, an evaporation gas suction unit 48, a remelting device 51, and a gas / liquid separator 60.

In this embodiment, in the fifth and sixth embodiments, the driving fluid supply line L2 is changed to the driving fluid supply line L11, the variable frequency driving pump 403, the forced vaporizer 404 are added, The regulating first valve B1, the supply control valve B2 and the flow regulating second valve B2 are omitted, and the rest of the configuration is the same as or similar to the first to eighth embodiments. The same or corresponding elements as those of the first to eighth embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 9 according to a ninth embodiment of the present invention will be described with reference to FIG.

The driving fluid supply line L11 may be branched between the booster pump 21 and the high pressure pump 22 and connected to the evaporation gas suction unit 48 and may be connected to the driving fluid supply line L11, A variable frequency drive pump 403 and a forced vaporizer 404 may be additionally provided.

Of course, in this case, valves (not shown) capable of adjusting the opening degree may be provided on the driving fluid supply line L11, and the supply amount of the liquefied gas may be controlled according to the opening degree control of each valve.

In the embodiment of the present invention, the liquefied gas is supplied through the variable-frequency drive pump 403 and the forced vaporizer 404 instead of the evaporation gas sucking unit 48, It is possible to control the amount of the evaporation gas sucked in the liquefied gas storage tank 20 without controlling the evaporation gas suction unit 48 on the driving fluid supply line L11 without providing an additional decompression device There is an effect that can be done.

The variable frequency drive pump 403 (VFD pump) is provided on the drive fluid supply line L11 and pressurizes the liquefied gas stored in the liquefied gas storage tank 20 and supplies it to the evaporation gas suction unit 48. [

The variable frequency drive pump 403 can supply and supply the liquefied gas supplied from the boosting pump 21 on the liquefied gas supply line L 1 to the evaporation gas suction unit 48 in a variable manner.

The forced vaporizer 404 is provided between the variable frequency drive pump 403 on the drive fluid supply line L11 and the evaporation gas suction unit 48 and vaporizes the liquefied gas supplied from the variable frequency drive pump 403 To the evaporation gas suction unit (48).

The forced vaporizer 404 here serves as a heat source for vaporizing the liquefied gas or a lubricant or seawater used in the propulsion engine 31 or the power generation engine 32 exhausted from the propulsion engine 31 or the power generation engine 32 And a separate heat source supply device (glycol water circulation system, etc.) can be used.

Thus, the gas treatment system 9 according to the present invention and the vessel containing the same effectively supply liquefied gas and / or evaporated gas from the liquefied gas storage tank 20 to the customers 31 and 51 to improve system stability and reliability Height is effective.

10 is a conceptual diagram of a gas processing system according to a tenth embodiment of the present invention.

10, the gas processing system 10 according to the tenth embodiment of the present invention includes a liquefied gas storage tank 20, a boosting pump 21, a high-pressure pump 22, a vaporizer 23, And includes a propulsion engine 31, a power generation engine 32, an evaporation gas suction unit 49, a liquid remover 51, a gas-liquid separator 60, a drive fluid supply line L12 and a sixth control unit 86 .

In this embodiment, in the fifth and sixth embodiments, the driving fluid supply line L2 is changed to the driving fluid supply line L12, and the third and fourth control units 84 and 84 are changed to the sixth control unit 86 And the flow control valve B1, the supply control valve B2 and the flow control valve B2 are changed to the first to third valves B6 to B8, And is configured to be the same as or similar to the ninth embodiment. The same or corresponding elements to those of the first to ninth embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 10 according to a tenth embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, the driving fluid supply line L12 is branched between the vaporizer 23 and the propulsion engine 31 of the liquefied gas supply line L1, and the first to third driving fluids And may include supply lines L12a, L12b, and L12c.

The first drive fluid supply line L12a can be branched between the vaporizer 23 of the liquefied gas supply line L1 and the propulsion engine 31 and connected to the evaporation gas suction unit 49, ).

Here, the first driving fluid supply line L12a may have a flow resistance of approximately 50 bar.

The second driving fluid supply line L12b may be branched in a direction between the vaporizer 23 and the propulsion engine 31 of the liquefied gas supply line L1 and provided in parallel with the first driving fluid supply line L12a And the other end may be connected to be joined to the first driving fluid supply line L12a.

Here, the second drive fluid supply line L12b may have a different flow resistance (resistance proportional to the friction coefficient of the line) than the first drive fluid supply line L12a. For example, the second drive fluid supply line L12b can realize a pressure of about 20 bar when the liquefied gas vaporized by the flow resistance is supplied to the evaporation gas suction unit 49. [

Further, the second driving fluid supply line L12b may include a second valve B7.

The third drive fluid supply line L12c is branched at one end between the vaporizer 23 and the propulsion engine 31 of the liquefied gas supply line L1 and connected to the first and second drive fluid supply lines L12a and L12b And the other end may be connected to be joined to the first driving fluid supply line L12a.

Here, the third drive fluid supply line L12c may be different from the flow resistance (resistance proportional to the friction coefficient of the line) as compared with the first and second drive fluid supply lines L12a and L12b. For example, The driving fluid supply line L12c can realize a subatmospheric pressure of about 10 bar when the liquefied gas vaporized by the flow resistance is supplied to the evaporation gas suction unit 49. [

In addition, the third drive fluid supply line L12c may include a third valve B8.

The first valve B6 to the third valve B8 may be connected to a sixth control unit 86 to be described later by wire or wirelessly to receive a drive instruction from the sixth control unit 86. [

The sixth control unit 86 can control the amount by which the evaporation gas sucking unit 49 sucks the evaporation gas in accordance with the internal pressure of the liquefied gas storage tank 20 through the first to third valves B6 to B8 have. Here, the sixth control unit 86 is connected to the first to third valves B6 to B8 by wire or wireless, and can transmit the opening adjustment driving instruction, and is connected to the detection sensor 81a by wire or wireless , And the internal pressure information of the liquefied gas storage tank (20).

Specifically, the sixth control unit 86 receives the internal pressure information of the liquefied gas storage tank 20 from the detection sensor 81a, and can control the opening of the first to third valves B6 to B8.

Hereinafter, the control operation of the sixth control unit 86 will be described in detail. For the sake of clarity, the valves controlled by the sixth control unit 86 are referred to as first to third valves B6 to B8, (B6 to B7).

The sixth control unit 86 closes the opening of the second valve B7 and releases only the opening of the first valve B6 when the internal pressure of the liquefied gas storage tank 20 is equal to or higher than the preset pressure, When the internal pressure of the liquefied gas storage tank 20 is lower than the predetermined pressure, the opening degree of each of the first and second valves B6 and B7 is controlled so that the pressure of the vaporized liquefied gas supplied to the unit 49 is increased. So that the pressure of the vaporized liquefied gas supplied to the evaporation gas suction unit 49 can be controlled to be low.

As a result, in the embodiment of the present invention, a separate pressure reducing device is not provided upstream of the evaporation gas suction unit 49, and instead, a plurality of driving fluid supply lines L12a, L12b, L12c The evaporation gas suction unit 49 can supply the liquefied gas to the liquefied gas storage tank 49 without providing a separate decompression device on the drive fluid supply lines L12a, L12b, and L12c, It is possible to control the amount of the evaporative gas sucked in the evaporator 20.

Thus, the gas treatment system 10 according to the present invention and the vessel containing the same effectively supply liquefied gas and / or evaporated gas from the liquefied gas storage tank 20 to the customer 31, 51, thereby improving system stability and reliability Height is effective.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the same is by way of illustration and example only and is not to be construed as limiting the present invention. It is obvious that the modification and the modification are possible.

It will be understood by those skilled in the art that various changes in form and details may be made therein without departing from the spirit and scope of the invention as defined by the appended claims.

1 to 10: Gas treatment system 20: Liquefied gas storage tank
21: boosting pump 22: high pressure pump
23: carburetor 31: propulsion engine
32: power generation engine 41 to 49: evaporation gas suction unit
401: forced vaporizer 402: buffer tank
403: variable frequency drive pump 404: forced vaporizer
51 to 52: Re-liquefier 60: Gas-liquid separator
71: Shaft generators 81 to 86: First to sixth control sections
81a: detection sensor
L1: liquefied gas supply line L2: drive fluid supply line
L3: Evaporative gas first branch line L4: Evaporative gas suction line
L5: evaporation gas supply line L6: first return line
L7: second return line L8: driving fluid supply line
L9: Evaporative gas suction line L10: Evaporative gas second branch line
L11: drive fluid supply line L12: drive fluid supply line
V1: first control valve V2: second control valve
B1: Flow regulating first valve B2: Supply control valve
B3: Flow regulating second valve B4: First valve
B5: second valve B6: first valve
B7: second valve B8: third valve
S: Propeller shaft P: Propeller

Claims (12)

A propulsion engine that receives liquefied gas from a liquefied gas storage tank and generates propulsion power of the ship;
A power generation engine that receives the liquefied gas and generates electric power to be used in the ship;
A liquefaction device for supplying liquefied gas to the liquefied gas storage tank at a pressure lower than a pressure required by the power generation engine;
And an evaporative gas suction unit for sucking and discharging the evaporative gas generated in the liquefied gas storage tank using the liquefied gas supplied to the propulsion engine as a driving fluid,
The evaporation gas sucking unit includes:
Wherein the evaporating gas to be discharged is supplied to the remanufacturing device so as not to supply the discharging evaporating gas to the power generation engine. The method according to claim 1,
A liquefied gas supply line connecting the liquefied gas storage tank and the propulsion engine;
A pump provided on the liquefied gas supply line for pressurizing the liquefied gas stored in the liquefied gas storage tank;
A vaporizer provided on the liquefied gas supply line for supplying a pressurized liquefied gas from the pump and vaporizing the liquefied gas;
A driving fluid supply line branched at the rear end of the vaporizer on the liquefied gas supply line and connected to the evaporation gas suction unit;
An evaporation gas suction line connecting the liquefied gas storage tank and the evaporation gas suction unit; And
Further comprising an evaporation gas supply line connecting the evaporation gas inlet unit and the refill liquefaction unit. 3. The method of claim 2,
The propulsion engine is a high pressure gas injection engine (MEGI) which consumes 200-400 bar of vaporized liquefied gas which is pressurized from the pump,
Characterized in that the power generation engine is a heterogeneous fuel engine which consumes 6 to 10 bar of evaporative gas. 4. The apparatus according to claim 3, wherein the evaporation gas sucking unit comprises:
A vaporized liquefied gas of 200 to 400 bar is supplied through the driving fluid supply line to suck the evaporation gas of 1 to 1.06 bar generated in the liquefied gas storage tank through the evaporation gas suction line, And a mixed fluid obtained by mixing the evaporation gas is discharged at a rate of 3 to 5 bar and supplied to the re-liquefier. 3. The method of claim 2,
And a precooler provided between the evaporation gas suction unit on the evaporation gas supply line and the refill liquefier and performing heat exchange between the liquefied gas supplied from the pump and the mixed fluid supplied from the evaporation gas suction unit. A vessel containing a gas treatment system. 6. The method according to claim 5, wherein the liquefied gas supply line
And a gas treatment system which is arranged to pass through said precooler. 3. The apparatus according to claim 2, wherein the evaporation gas supply line includes:
Wherein the vaporizer is arranged to pass through the vaporizer. 2. The liquefaction apparatus according to claim 1,
Wherein the evaporating gas is supplied to the liquefied gas storage tank by re-liquefying the entire evaporation gas discharged from the evaporation gas suction unit through a separate refrigerant. 9. The method of claim 8,
A return line connecting the liquefaction device and the liquefied gas storage tank; And
Further comprising a gas-liquid separator provided on the return line and separating the liquefied evaporated gas supplied from the remelting device into vapor and liquid. The method according to claim 1,
Further comprising a shaft generator connected to a drive shaft of the propulsion engine and generating at least part of the power generated by the propulsion engine and generating electric power,
And supplies power generated in the shaft generator to the remelting device. The power generation system according to claim 1,
And supplies the generated power to the remelting device. The method according to claim 1,
The propulsion engine is a low pressure gas injection engine (XDF)
Characterized in that the power generation engine is a heterogeneous fuel engine which consumes 6 to 10 bar of evaporative gas.

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