KR20150030938A - Apparatus for the reliquefaction of boil-off gas - Google Patents

Apparatus for the reliquefaction of boil-off gas Download PDF

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Publication number
KR20150030938A
KR20150030938A KR20130110290A KR20130110290A KR20150030938A KR 20150030938 A KR20150030938 A KR 20150030938A KR 20130110290 A KR20130110290 A KR 20130110290A KR 20130110290 A KR20130110290 A KR 20130110290A KR 20150030938 A KR20150030938 A KR 20150030938A
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South Korea
Prior art keywords
refrigerant
gas
unit
heat
cooling
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KR20130110290A
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Korean (ko)
Inventor
이원두
윤호병
이종철
인세환
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삼성중공업 주식회사
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Priority to KR20130110290A priority Critical patent/KR20150030938A/en
Publication of KR20150030938A publication Critical patent/KR20150030938A/en

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C13/00—Details of vessels or of the filling or discharging of vessels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C5/00—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures
    • F17C5/02—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures for filling with liquefied gases
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C6/00—Methods and apparatus for filling vessels not under pressure with liquefied or solidified gases

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

An apparatus for the reliquefaction of boil-off gas is disclosed. According to an embodiment of the present invention, the apparatus for the reliquefaction of boil-off gas comprises a storage unit for storing LNG; a boil-off gas (BOG) compression cooling unit which has one or more BOG compressors for receiving and compressing BOG generated in the storage unit and one or more BOG coolers for cooling BOG; a reliquefaction unit for the reliquefaction of BOG by circulating a refrigerant to exchange heat with BOG compressed in the BOG compression cooling unit; a cold and heat recovery unit for connecting the storage unit to the BOG compressors to recover the cold and heat of BOG by exchanging heat with the reliquefaction unit; and a fuel supply unit for supplying the BOG, which has passed through the reliquefaction unit, to the engine of a ship as a fuel.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to an evaporation gas re-

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an evaporation gas remelting apparatus, and more particularly, to an evaporation gas remelting apparatus capable of reducing energy consumed in re-liquefying an evaporation gas by recovering cold and heat of the evaporation gas.

In general, natural gas is transported through the pipeline to the gaseous state while moving from place of production to use.

When natural gas is transported by sea, it is liquefied in a high-pressure / low-temperature environment and transported over an LNG carrier by a large volume when it is transported to the gaseous state.

The transported liquefied natural gas is maintained at a cryogenic temperature of -162 ° C in the LNG storage tank of the LNG carrier.

However, as the LNG carriers are shaken during transportation, evaporation gas (BOG, Boil-Off-Gas) is continuously generated in the LNG storage tank by the flow of liquefied gas, temperature gradient, cooling process,

That is, since the liquefaction temperature of natural gas is a cryogenic temperature of about -162 ° C at normal pressure, LNG is evaporated even if its temperature is slightly higher than -162 ° C at normal pressure.

Although the LNG storage tank of the LNG carrier is adiabatically treated, the external heat is continuously transferred to the LNG, so that during the transportation of the LNG by the LNG carrier, the LNG is constantly vaporized in the LNG storage tank and stored in the LNG storage tank Evaporation gas is generated.

The generated evaporation gas increases the pressure inside the LNG storage tank and accelerates the flow of the liquefied gas in accordance with the shaking motion of the ship, which may cause structural problems, so it is necessary to suppress the generation of the evaporation gas.

An LNG carrier that does not have a liquefaction device blows evaporative gas, which is continuously generated during transportation, to the air through combustion or the like.

As a result, the final destination is transported with a loss of significant natural gas loss compared to the original natural gas reserves.

In order to reduce the loss of natural gas, LNG carriers are equipped with an evaporative gas re-liquefaction device, which is an evaporative gas recovery device.

In addition, LNG RV (Regasification Vessel), LNG FPSO (Floating, Production, Storage and Off-loading) and LNG FSRU (Floating Storage and Regasification Unit) And recovering evaporative gas generated during storage.

For reference, LNG RV is a LNG regeneration facility installed on a liquefied gas carrier capable of self-propulsion and floating, and LNG FPSO is a liquefied natural gas that is directly liquefied after being refined in the sea and stored in a storage tank. LNG FSRU is a maritime structure used to transport LNG stored in a tank to an LNG carrier. LNG FSRU stores liquefied natural gas unloaded from an LNG carrier offshore at sea and stores it in a storage tank, It is the offshore structure that supplies to the demand of the land.

 The evaporative gas re-liquefying apparatus currently being developed liquefies the evaporation gas by discharging the evaporation gas to the outside of the LNG storage tank and liquefying the evaporation gas by using the refrigerant, or by pressurizing the evaporation gas, cooling it to room temperature, and then expanding it under reduced pressure.

 However, when the evaporation gas is liquefied by using the refrigerant, the liquefaction of the natural gas consumes a lot of energy because it must be cooled down to -162 ° C or less at 1 atm, which is the storage pressure of the LNG tank.

Also, the process of pressing the evaporation gas and cooling it to room temperature uses a compressor. Thereafter, in order to return to the LNG storage tank, the flash gas is generated in a process of decompression expansion, The energy efficiency of the ship is lowered.

On the other hand, in recent years, environmental regulations such as emission gas management have been strengthened in connection with the emission of pollutants from ships.

Thus, shipbuilders can use DF (Dual-Fuel) engine, which can use both natural gas and marine diesel fuel, or ME-GI (Man Electric-driven Gas Injection) engine, which is a two- And is trying to build eco-friendly vessels.

Accordingly, when a high-pressure gas injection engine (ME-GI engine or the like) capable of using BOG or LNG as fuel for a ship or an offshore structure having LNG storage device is used, it has an advantage of being able to cope with environmental regulations.

The re-liquefaction device and the high-pressure natural gas injection engine fuel supply device in a ship or an offshore structure having a conventional LNG storage device were independently developed.

In recent years, however, a process has been developed that increases energy efficiency with the combined design of the two devices.

This development process generally involves adding a high-pressure natural gas fueling device to the refueling device.

In this case, the evaporation gas is re-liquefied by compressing / expanding the nitrogen by using nitrogen as a refrigerant.

This re-liquefying device is disadvantageous in that the refrigerant nitrogen is used for absorbing heat generated during the evaporation gas compression, resulting in low energy efficiency.

In addition, heat exchange between the liquefaction device and the fuel supply device is not utilized, so that waste heat can not be recovered and consequently, the energy consumption of the ship can not be reduced.

 Korean Public Release No. 10-2009-0020574 (Published on February 26, 2009)

SUMMARY OF THE INVENTION Accordingly, it is an object of the present invention to provide an evaporative gas re-liquefying apparatus capable of reducing the energy consumed in re-liquefaction of evaporated gas by recovering the cold heat of the evaporated gas generated in the place where the liquefied natural gas is stored .

According to an aspect of the present invention, there is provided a gas turbine comprising: a storage unit storing liquefied natural gas; An evaporation gas compression cooling unit comprising at least one evaporative gas compressor for supplying and compressing boil-off-gas (BOG) generated in the storage unit, and at least one evaporative gas cooler for cooling the evaporative gas; A re-liquefaction unit for circulating the refrigerant for heat exchange with the evaporated gas compressed in the evaporative gas compression and cooling unit, and liquefying the evaporated gas; A cold / hot water collecting unit connecting the storage unit and the evaporative gas compressor, wherein the cold / hot water recovering unit exchanges heat with the redistribution unit to recover cold heat of the evaporated gas; And a fuel supply unit for supplying the evaporative gas that has passed through the resupply unit to the engine of the ship as fuel.

The re-liquefaction unit comprises: at least one refrigerant compressor for compressing the refrigerant; One or more refrigerant coolers for cooling the refrigerant passing through the refrigerant compressor; A refrigerant inflator for expanding the volume of the refrigerant passing through the refrigerant cooler and for cooling the temperature; And a re-liquefying heat exchanger for exchanging heat with the refrigerant having passed through the refrigerant inflator and the evaporation gas passing through the evaporation gas compression and cooling unit to liquefy the evaporation gas.

The re-liquefaction unit may further include a refrigerant heat exchanger for exchanging heat between the refrigerant passing through the refrigerant cooler and the refrigerant before the refrigerant compressor.

The heat recovery unit may exchange heat with the re-liquefaction unit between the refrigerant cooler and the refrigerant heat exchanger.

Wherein the fuel supply unit comprises: a drum in which the evaporation gas passes through the remelting heat exchanger and is liquefied and stored; A pump for pressurizing the evaporative gas not stored in the storage unit to be used as fuel for the engine of the ship; And an evaporator for evaporating the evaporation gas.

And an evaporation gas heat exchanger that connects the pump and the evaporator and cools the evaporation gas that has passed through the evaporation gas compression and cooling unit by heat exchange.

In the evaporative gas compression unit, the evaporative gas compressor and the evaporative gas cooler may be provided in multiple stages, and the refrigerant compressor and the refrigerant cooler may be provided in multiple stages in the re-liquefier unit.

Embodiments of the present invention can reduce the energy consumed in re-liquefying the evaporated gas by recovering the cold heat of the evaporated gas generated at the place where the liquefied natural gas is stored.

1 is a configuration diagram of an evaporation gas remelting apparatus according to an embodiment of the present invention.
2 is a configuration diagram of an evaporation gas remelting apparatus according to another embodiment of the present invention.

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

Hereinafter, the present invention will be described in detail with reference to the preferred embodiments of the present invention with reference to the accompanying drawings. Like reference symbols in the drawings denote like elements.

Fig. 1 is a configuration diagram of an evaporation gas remelting apparatus 1 according to an embodiment of the present invention, and Fig. 2 is a configuration diagram of an evaporation gas remelting apparatus 1a according to another embodiment of the present invention.

Hereinafter, the configuration of the evaporation gas remelting device 1 will be described first, and then the flow of the evaporation gas and the refrigerant will be described.

1, an evaporation gas remelting apparatus 1 according to an embodiment of the present invention includes a storage unit 100 storing liquefied natural gas, an evaporation gas compression cooling unit 200, A heat recovery unit 400 for recovering evaporative gas cold and heat and a fuel supply unit 500 for supplying fuel to the engine 700 of the ship.

First, the storage unit 100 represents an LNG storage tank storing LNG (Liquefied Natural Gas).

Generally, as the LNG carriers oscillate, evaporation gas may continuously be generated in the storage unit 100 due to the flow of liquefied natural gas, the temperature gradient of the LNG storage tank, and the cooling process of the LNG storage tank.

For reference, in the present embodiment, the re-liquefier 1 is applied to an LNG carrier, but the LNG RV, the LNG FPSO, the LNG FSRU having the LNG storage tank, It will be appreciated that the device 1 may be applied.

Next, the evaporation gas compression and cooling unit 200 serves to compress the evaporation gas generated in the storage unit 100 and to cool it again.

Thus, the evaporative gas compression cooling unit 200 includes at least one evaporative gas compressor 220 and at least one evaporative gas cooler 240 to compress and cool the evaporative gas.

In this embodiment, the evaporative gas compression cooling unit 200 includes two evaporative gas compressors 220 and two evaporative gas coolers 240, in which the evaporative gas compressor 220 and the evaporative gas cooler 240 alternately .

However, the scope of the present invention is not limited thereto, and the number of the evaporative gas compressor 220 and the evaporative gas cooler 240 may be appropriately selected.

Thus, the evaporative gas compression cooling unit 200 may be provided with only one evaporative gas compressor 220 and one evaporative gas cooler 240, or in three or more multi-stages.

The re-liquefier unit 300 has a refrigerant for heat exchange with the evaporated gas compressed in the evaporative gas compression and cooling unit 200, and functions to heat the evaporated gas by exchanging heat between the evaporated gas and the refrigerant.

This re-liquefaction unit 300 includes one or more refrigerant compressors 320, one or more refrigerant coolers 340, a refrigerant inflator 360, and a remelting heat exchanger 380.

In this embodiment, the re-liquefier unit 300 includes three refrigerant compressors 320 and three refrigerant compressors 340, in which the refrigerant compressors 320 and the refrigerant compressors 340 are arranged alternately.

However, the scope of the present invention is not limited thereto, and the number of the refrigerant compressors 320 and the refrigerant compressors 340 may be appropriately selected.

 Thus, the re-liquefier unit 300 may be provided with only one refrigerant compressor 320 and one refrigerant compressor 340, or two or four or more multi-stage refrigerant compressors.

The refrigerant compressor 320 serves to compress the refrigerant, and the refrigerant cooler 340 serves to cool the refrigerant that has passed through the refrigerant compressor 320 again.

The refrigerant inflator 360 serves to expand the volume of the refrigerant passing through the refrigerant cooler 340 to lower the temperature of the refrigerant.

Accordingly, the refrigerant compressor 320 and the refrigerant cooler 340 are provided in multiple stages in the present embodiment, and as a result, the compression / cooling efficiency can be increased.

Meanwhile, in the present embodiment, nitrogen is used as an example of the refrigerant, but it is natural that an inert gas such as hydrocarbon or argon and a mixed refrigerant can be applied as the refrigerant.

The refrigerant is injected into the liquefaction heat exchanger 380 at a low temperature of about -165 DEG C to re-liquefy the evaporation gas.

The re-liquefying heat exchanger 380 functions to heat the refrigerant passing through the refrigerant inflator 360 and the evaporation gas passing through the evaporation gas compression and cooling unit 200 to liquefy the evaporation gas.

The re-liquefier unit 300 further includes a refrigerant heat exchanger 390 for exchanging the refrigerant that has passed through the refrigerant cooler 340 and the refrigerant before passing through the refrigerant compressor 320.

The refrigerant heat exchanger 390 exchanges heat between the refrigerant that has passed through the re-liquefying heat exchanger 380 and the refrigerant that has passed through the refrigerant cooler 340, thereby recovering the waste heat of the refrigerant.

Next, the cold / hot water recovering unit 400 may include a conduit 411 connected to the storage unit 100 and a cold / hot water heat exchanger 410 exchanging heat with the liquid remoaking unit 300.

Therefore, the cold / hot water collection unit 400 connects the storage unit 100 and the evaporative gas compressor 220, and performs heat exchange with the redistribution unit 300 to recover cold and hot of the evaporated gas.

Thus, the energy consumed in re-liquefying the evaporated gas can be reduced.

The cold / hot water heat exchanger 410 may be disposed at a plurality of locations, but in the present embodiment, it is located between the coolant cooler 340 and the refrigerant heat exchanger 390.

In this case, there is an advantage that the cold heat of the evaporation gas can be efficiently recovered at an early stage.

Meanwhile, the fuel supply unit 500 includes a drum 520 stored by liquefying the evaporation gas, a pump 540 serving to transfer the evaporation gas to the engine 700 of the ship, (560).

The drum 520 is a place where the evaporated gas is liquefied and temporarily stored after passing through the remelting heat exchanger 380.

A part of the liquefied evaporated gas is moved to the pump 540 and the liquefied evaporated gas not moved to the pump 540 is moved to the storage unit 100 again.

The pump 540 serves to pressurize liquefied evaporative gas not stored in the storage unit 100 to be used as fuel for the engine 700 of the ship.

The evaporator 560 serves to evaporate the liquefied evaporative gas to supply it to the engine 700 of the ship.

If LNG is not loaded in the LNG carriers, the amount of evaporation gas may be very small or not generated.

Therefore, at this time, the natural gas stored in the storage unit 100 must be used for driving the engine 700 of the ship.

Therefore, the storage pump 110 functions to pressurize the liquid natural gas from the storage unit 100 to be suitable for use in the engine 700 of the ship.

Hereinafter, the flow of the evaporation gas and the refrigerant according to one embodiment of the present invention will be described.

First, the evaporation gas is generated in the LNG gas stored in the storage unit 100.

The generated evaporated gas flows along the conduit 411 of the cold heat recovery unit 400 and flows to the cold recovery heat exchanger 410. [

The evaporated gas flowing into the cold / hot water heat exchanger 410 first exchanges heat with the refrigerant passing through the refrigerant cooler 340, and as a result, the cold / hot of the evaporated gas is recovered.

Thus, the energy consumed in re-liquefying the evaporated gas can be reduced.

Thus, the heated evaporated gas passes through the evaporated gas compressor 220 and the evaporated gas cooler 240, respectively, so that the pressure rises.

Then, the high-pressure evaporation gas is heat-exchanged with the refrigerant using the re-liquefying heat exchanger 380.

Next, referring to the flow of the refrigerant, the refrigerant is injected into the re-liquefying heat exchanger 380 in a state of -165 ° C before re-liquefaction, and unlike the conventional case, the evaporated gas compressed by the evaporating gas compressor 220 is not cooled .

The refrigerant having passed through the re-liquefying heat exchanger 380 is then compressed and cooled through the refrigerant compressor 320 and the refrigerant cooler 340.

The compressed and cooled refrigerant passes through the cold heat recovery heat exchanger 410 and primarily exchanges heat with the low-temperature evaporated gas, and as a result, the temperature is lowered.

Thereafter, the refrigerant secondarily exchanges heat between the refrigerant passing through the refrigerant cooler 340 and the refrigerant passing through the re-liquefying heat exchanger 380 by the refrigerant heat exchanger 390 recovering the waste heat of the refrigerant, As a result, the temperature of the refrigerant drops to a lower temperature than the conventional one.

The refrigerant having such a low temperature passes through the refrigerant inflator 360 and decompresses and expands, and the temperature is lowered in the third order.

That is, according to the present invention, as the first cooling process is added in advance, the refrigerant is lowered to a temperature of -165 ° C or lower, and the reduced pressure is lowered.

 Accordingly, the pressure range to be compressed by the multi-stage refrigerant compressors 320 can be reduced to reduce the energy used in the refrigerant compressors 320, and the sizes of the multi-stage refrigerant compressors 320 and the multi-stage refrigerant compressors 340 can be reduced.

On the other hand, FIG. 2 shows an evaporative gas remelting apparatus 1a according to another embodiment of the present invention.

In the evaporation gas remelting device 1a of another embodiment of the present invention, description of the same constitution as that of the evaporation gas remelting device 1 of the embodiment of the present invention has been described above, and the other constitution will be described.

As shown in Fig. 2, the evaporation gas remelting device 1a of another embodiment of the present invention further includes an evaporation gas heat exchanger 600. Fig.

The evaporation gas heat exchanger 600 is provided between the pump 540 and the evaporator 560.

The evaporation gas heat exchanger 600 is stored in the storage unit 100 and serves to exchange heat between the liquid natural gas pressurized by the pump 540 and the evaporated gas passing through the evaporative gas cooler 240.

The natural gas stored in the storage unit 100 should be used for driving the engine 700 of the ship when the amount of the generated gas is very small or does not occur when the LNG carrier is not loaded in the LNG carrier .

Therefore, the liquid natural gas stored in the storage unit 100 is pressurized by the storage pump 110, and is heat-exchanged with the evaporative gas passing through the evaporative gas cooler 240 in the evaporative gas heat exchanger 600, And the efficiency of the re-liquefied energy is increased.

Hereinafter, the flow of the evaporation gas and the refrigerant of the evaporation gas remelting apparatus 1a according to another embodiment of the present invention will be described.

First, the evaporation gas is generated in the LNG gas stored in the storage unit 100.

The generated evaporated gas flows along the conduit 411 of the cold / hot water recovering unit 400 and flows to the cold / hot water recovering heat exchanger 410.

The evaporated gas flowing into the cold / hot water heat exchanger (410) is first heat-exchanged with the refrigerant passed through the refrigerant cooler (340), and the cold heat of the evaporated gas is recovered.

Thus, the heated evaporated gas passes through the evaporated gas compressor 220 and the evaporated gas cooler 240, respectively, so that the pressure rises.

The high-pressure evaporation gas is heat-exchanged with the liquid natural gas by using the evaporation gas heat exchanger 600 to perform the primary cooling.

In this case, when the amount of evaporated gas generated in the storage unit 100 is small, the stored liquid natural gas is pressurized by the storage pump 110, and the evaporated gas cooler 240 The efficiency of the re-liquefied energy is increased.

Thereafter, the evaporated gas at a high pressure is subjected to heat exchange with the refrigerant using the re-liquefying heat exchanger 380, thereby performing liquefaction through secondary cooling.

Next, referring to the flow of the refrigerant, the refrigerant is injected into the re-liquefying heat exchanger (380), and is heat-exchanged with the evaporated gas passing through the evaporating gas heat exchanger (600).

The refrigerant having passed through the re-liquefying heat exchanger 380 is then compressed and cooled through the refrigerant compressor 320 and the refrigerant cooler 340 at the multi-stage.

The compressed and cooled refrigerant passes through the cold heat recovery heat exchanger 410 and is heat-exchanged with the low temperature evaporation gas, so that the temperature is lowered.

The refrigerant passing through the cold / hot water heat exchanger 410 is heat-exchanged with the low temperature evaporated gas generated in the LNG storage tank by the refrigerant heat exchanger 390, and the temperature is lowered.

The refrigerant having such a low temperature passes through the refrigerant inflator 360, decompresses and expands, and is continuously circulated.

In other words, the evaporation gas re-liquefying apparatus 1a according to another embodiment of the present invention is different from the evaporation gas re-liquefaction apparatus 1 according to the embodiment of the present invention in that the liquid natural And a process of recovering the cold heat of the liquid natural gas by pressurizing the gas with the storage pump 110 is added.

 It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit or scope of the invention. Accordingly, such modifications or variations are intended to fall within the scope of the appended claims.

100: storage unit 200: evaporation gas compression cooling unit
300: re-liquefying unit 400: cold /
500: fuel supply unit 600: evaporative gas heat exchanger
700: Engine 1: Liquefaction device

Claims (7)

A storage unit for storing liquefied natural gas;
An evaporation gas compression cooling unit comprising at least one evaporative gas compressor for supplying and compressing boil-off-gas (BOG) generated in the storage unit, and at least one evaporative gas cooler for cooling the evaporative gas;
A re-liquefaction unit for circulating the refrigerant for heat exchange with the evaporated gas compressed in the evaporative gas compression and cooling unit, and liquefying the evaporated gas;
A cold / hot water recovering unit connecting the storage unit and the evaporative gas compressor to heat-exchange with the re-liquefier unit to recover cold heat of the evaporated gas; And
And a fuel supply unit for supplying the evaporative gas that has passed through the resupply unit to the engine of the ship as fuel. The method according to claim 1,
The re-liquefying unit includes:
One or more refrigerant compressors for compressing the refrigerant;
One or more refrigerant coolers for cooling the refrigerant passing through the refrigerant compressor;
A refrigerant inflator for expanding the volume of the refrigerant passing through the refrigerant cooler and for cooling the temperature; And
And a liquefaction heat exchanger for exchanging heat with the refrigerant having passed through the refrigerant inflator and the evaporation gas passing through the evaporation gas compression and cooling unit to liquefy the evaporation gas. 3. The method of claim 2,
The re-liquefying unit includes:
And a refrigerant heat exchanger for exchanging heat between the refrigerant passed through the refrigerant cooler and the refrigerant before the refrigerant compressor. The method of claim 3,
The cold /
And the heat exchanging unit exchanges heat with the re-liquefier unit between the refrigerant cooler and the refrigerant heat exchanger. 5. The method of claim 4,
The fuel supply unit includes:
A drum through which the evaporation gas is passed through the remelting heat exchanger to be liquefied and stored;
A pump for pressurizing the evaporative gas not stored in the storage unit to be used as fuel for the engine of the ship; And
And an evaporator for evaporating the evaporation gas. 6. The method of claim 5,
And an evaporation gas heat exchanger for connecting the pump and the evaporator and for cooling the evaporation gas passing through the evaporation gas compression and cooling unit by heat exchange. 3. The method of claim 2,
In the evaporative gas compression cooling unit, the evaporative gas compressor and the evaporative gas condenser are provided in multiple stages,
And the refrigerant compressor and the refrigerant cooler are provided in multiple stages in the re-liquefaction unit.
KR20130110290A 2013-09-13 2013-09-13 Apparatus for the reliquefaction of boil-off gas KR20150030938A (en)

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20170004697A (en) * 2015-07-03 2017-01-11 대우조선해양 주식회사 Control System Of Boil Off Gas Treatment System
KR20190137693A (en) * 2018-06-01 2019-12-11 가부시키가이샤 고베 세이코쇼 Gas supply system

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20170004697A (en) * 2015-07-03 2017-01-11 대우조선해양 주식회사 Control System Of Boil Off Gas Treatment System
KR20190137693A (en) * 2018-06-01 2019-12-11 가부시키가이샤 고베 세이코쇼 Gas supply system

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