KR101739986B1 - Boil Off Gas Reliquefaction System And Method - Google Patents

Boil Off Gas Reliquefaction System And Method Download PDF

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KR101739986B1
KR101739986B1 KR1020150060310A KR20150060310A KR101739986B1 KR 101739986 B1 KR101739986 B1 KR 101739986B1 KR 1020150060310 A KR1020150060310 A KR 1020150060310A KR 20150060310 A KR20150060310 A KR 20150060310A KR 101739986 B1 KR101739986 B1 KR 101739986B1
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South Korea
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bog
refrigerant
lng
compressed
line
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KR1020150060310A
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Korean (ko)
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KR20160128635A (en
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윤상득
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대우조선해양 주식회사
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
    • B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
    • B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
    • B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
    • B63B25/16—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed heat-insulated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63H—MARINE PROPULSION OR STEERING
    • B63H21/00—Use of propulsion power plant or units on vessels
    • B63H21/38—Apparatus or methods specially adapted for use on marine vessels, for handling power plant or unit liquids, e.g. lubricants, coolants, fuels or the like
    • 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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • F17C2265/033—Treating the boil-off by recovery with cooling
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/06—Fluid distribution
    • F17C2265/066—Fluid distribution for feeding engines for propulsion
    • 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
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/0105—Ships
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
    • Y02T70/00—Maritime or waterways transport
    • Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system
    • Y02T70/5218—Less carbon-intensive fuels, e.g. natural gas, biofuels

Abstract

A vapor gas remelting system and method are disclosed. The boil-off gas re-liquefaction system of the present invention comprises a BOG re-liquefaction line for compressing and cooling BOG (Boil-Off Gas) generated in an LNG storage tank provided in a ship or an offshore structure to re- A refrigerant circulation line through which the refrigerant for cooling the BOG circulates; A compander provided in the BOG re-liquefaction line and including an expander for receiving and expanding the refrigerant, and a BOG compressor for compressing the BOG using the expansion force of the refrigerant in the expander; A main heat exchanger for cooling the compressed BOG by heat exchange with the refrigerant which is thermally expanded in the expander; A booster compressor provided in the BOG re-liquefaction line for supplying the compressed BOG from the BOG compressor to the main heat exchanger; And a fuel supply line for branching the BOG compressed from the downstream of the compander in the BOG re-liquefaction line, mixing the re-condensed LNG supplied from the LNG storage tank, compressing and forcing the fuel into the high- And a control unit.

Figure R1020150060310

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a boil-

More particularly, the present invention relates to a system and method for re-liquefying an evaporative gas, and more particularly, to a system and method for re-liquefying an evaporative gas, The present invention relates to a system and a method for liquefying a vaporized gas that can be processed by re-liquefaction by cooling the compressed BOG by heat exchange with the cooled refrigerant.

In recent years, consumption of liquefied gas such as LNG (Liquefied Natural Gas) and LPG (Liquefied Petroleum Gas) has been rapidly increasing worldwide. The liquefied gas obtained by liquefying the gas at a low temperature has an advantage of being able to increase the storage and transport efficiency because the volume becomes very small as compared with the gas. In addition, liquefied natural gas (Liquefied Natural Gas) (hereinafter referred to as "LNG") can be used as an eco-friendly fuel which can remove or reduce air pollutants during the liquefaction process,

For example, liquefied natural gas is a colorless transparent liquid which can be obtained by cooling natural gas containing methane as a main component to about -162 ° C and liquefying it, and has a volume of about 1/600 as compared with natural gas. Therefore, it can be transported very efficiently when liquefied by LNG for transporting natural gas.

However, since the liquefaction temperature of natural gas is a cryogenic temperature of -162 ° C at normal pressure, LNG is sensitive to temperature change and is easily evaporated. As a result, the LNG storage tank of the LNG carrier is insulated. However, since the external heat is continuously transferred to the LNG storage tank, the LNG is continuously vaporized in the LNG storage tank during the LNG transportation, BOG) occurs. This also applies to other low temperature liquefied gases such as ethane.

BOG is a kind of loss and an important issue in transportation efficiency. Further, when the evaporation gas accumulates in the storage tank, the internal pressure of the tank may rise excessively, and there is a risk that the tank may be damaged. Therefore, various methods for treating BOG occurring in the storage tank have been studied. Recently, a method of re-liquefying BOG to return to a storage tank for processing BOG, a method of returning BOG to a storage tank, And the like are used.

The present applicant has proposed a re-liquefying apparatus which utilizes the cooling heat of the evaporation gas itself by using the evaporation gas as the cooling fluid on Jul. 10, 2013, No. 10-2013-0081029. The Partial Re-liquefaction System (PRS) proposed in the patent of No. 10-2013-0081029 is a device for re-liquefying the evaporated gas discharged outside the storage tank by using the evaporation gas itself as a refrigerant, It is possible to re-liquefy the evaporated gas without separately installing the re-liquefier, and it is evaluated as an epoch-making technology that can effectively reduce the overall natural evacuation rate (BOR) of the liquefied natural gas storage tank.

1 is a schematic configuration diagram of the redispersion apparatus of the present invention, No. 10-2013-0081029. Referring to FIG. 1, the process of re-liquefying the evaporation gas in the re-liquefier will be briefly described below.

The evaporated gas discharged from the storage tank 10 can be compressed through a multi-stage compressor including a plurality of compressors 30 and an intercooler (not shown). In the compressor shown in FIG. 1, five stages of compression and cooling are alternately performed while passing through five compressors 30, and are compressed. Some of the evaporated gas that has undergone the compression process is sent to a high-pressure fuel consuming station E1 requiring high-pressure fuel, for example, a high-pressure engine such as an ME-GI engine, Lt; / RTI > The evaporation gas (A line) supplied to the heat exchanger 20 through the multi-stage compression process is heat-exchanged in the heat exchanger 20 with the evaporation gas (B line) discharged from the storage tank 10 and introduced into the compressor. The temperature of the evaporation gas is increased through the compression process, so that the evaporation gas before compression discharged from the storage tank 10 is used as the refrigerant for cooling the compressed evaporation gas.

The evaporated gas (C line) cooled through heat exchange in the heat exchanger 20 after the compression is decompressed in the decompressor 40. At least a part of the evaporated gas compressed while passing through the heat exchanger (20) and the pressure reducing device (40) is re-liquefied. In the gas-liquid separator 50, the re-liquefied liquefied natural gas is separated from the evaporated gas remaining in the gaseous state, and the re-liquefied evaporated gas is returned to the storage tank 10, and the evaporated gas (D line) (B line) discharged from the storage tank 10 to the heat exchanger 20 again.

In the case where there is a low-pressure fuel consuming place which is supplied with a gas of lower pressure than the gas which has passed through all the multi-stage compressors in a ship, for example, three of the five compressors 30, And can be supplied as fuel to the fuel consumption destination E2. Further, when the amount of evaporative gas generated from the storage tank 10 is large and is supplied as fuel for the high-pressure and low-pressure fuel consuming destination and remains after liquefaction by the partial re-liquefier, venting or gas- ; Gas Combustion Unit) to incinerate.

The present applicant's prior art is a device capable of effectively treating evaporative gas generated in a storage tank. In order to constitute such a device, an expensive compressor or the like is constituted, so that a facility cost is high. In particular, And the operating cost was also high.

The present invention solves the above problem and proposes a vaporization gas re-liquefaction system that can more effectively compress BOG and re-liquefy and process it.

According to an aspect of the present invention, there is provided a BOG re-liquefaction line for re-liquefaction by compressing and cooling BOG (Boil-Off Gas) generated in an LNG storage tank provided in a ship or an offshore structure;

A refrigerant circulation line through which the refrigerant for cooling the BOG circulates;

A compander provided in the BOG re-liquefaction line and including an expander for receiving and expanding the refrigerant, and a BOG compressor for compressing the BOG using the expansion force of the refrigerant in the expander;

A main heat exchanger for cooling the compressed BOG by heat exchange with the refrigerant which is thermally expanded in the expander;

A booster compressor provided in the BOG re-liquefaction line for supplying the compressed BOG from the BOG compressor to the main heat exchanger; And

A BOG re-liquefaction line is connected to the LNG storage tank, and the BOG is branched from the LNG storage tank, and the BOG is mixed with the LNG supplied from the LNG storage tank and recycled, compressed and forcedly vaporized, An evaporative gas re-liquefaction system is provided.

Preferably, the refrigerant compressor is provided in the refrigerant circulation line and receives and compresses the refrigerant discharged from the main heat exchanger after heat exchange with the BOG. And

And a refrigerant precooler provided in the refrigerant circulation line for cooling the refrigerant compressed by the refrigerant compressor and supplying the refrigerant to the expander.

Preferably, in the refrigerant precooler, the uncompressed refrigerant to be introduced into the refrigerant compressor, the BOG generated from the LNG storage tank to be supplied to the BOG compressor, the LNG recondensed and compressed in the fuel supply line, And the coolant may be cooled by heat exchange with at least one of flash gas generated during recondensing of the BOG in the fuel supply line.

Preferably, decompression means provided in the BOG liquefaction line and depressurizing the BOG cooled in the main heat exchanger or the LNG generated from the BOG; And

And a flash drum provided in the BOG liquefaction line and supplying the BOG or LNG, which is decompressed by the decompression unit, to a gas-liquid separation.

Preferably, the BOG compressed by the BOG compressor of the compander may be supplied as fuel to a low-pressure fuel consuming place provided in the vessel or the offshore structure.

A recondenser provided in the fuel supply line and supplied with the BOG branched from the front end or the rear end of the booster compressor to mix and cool the LNG supplied from the LNG storage tank;

A high pressure pump which is provided in the fuel supply line and receives LNG from the re-condenser and compresses the LNG at a supply pressure of the high pressure gas consuming place; And

And a carburetor provided in the fuel supply line for forcibly vaporizing the LNG compressed by the high-pressure pump.

A fuel heating line branched from the fuel supply line at a rear end of the high pressure pump and connected to the fuel supply line from the front end of the vaporizer via the refrigerant precooler; And

And a flash gas supply line for supplying a flash gas generated when the BOG and LNG are mixed in the re-condenser to the upstream of the compander of the BOG re-liquefaction line.

Preferably, the refrigerant circulating through the refrigerant circulation line may be at least one of BOG, nitrogen (N 2 ), and mixed refrigerant including methane.

According to another aspect of the present invention, there is provided a method of controlling a boiler system comprising the steps of: 1) supplying a boil-off gas (BOG) generated in an LNG storage tank provided on a ship or a marine structure to a compander including an expander and a BOG compressor; ;

2) compressing the BOG in the BOG compressor using the expanding force of the refrigerant in the expander while receiving the refrigerant in the expander of the compander and performing the thermal expansion;

3) supplying the compressed BOG to the booster compressor and further compressing it to a pressure higher than the critical pressure; And

4) supplying the compressed BOG to the main heat exchanger, cooling the refrigerant by heat exchange with the refrigerant discharged after being thermally expanded from the expander to re-liquefy,

Wherein the compressed BOG is branched from the downstream of the compander and is mixed with LNG supplied from the LNG storage tank to be recycled and compressed and forcedly vaporized so as to be supplied as fuel for the high pressure gas consuming area, Method is provided.

Preferably, the refrigerant is compressed and cooled and supplied to the expander, wherein the refrigerant is generated from the uncompressed refrigerant, the LNG storage tank, and the BOG to be supplied to the BOG compressor, Through the heat exchange with at least one of the recondensed and compressed LNG after branching from the downstream of the LNG and flash gas occurring upon re-condensation of the BOG which is diverted for fuel supply.

The BOG generated in the LNG storage tank can be effectively re-liquefied and stored through the system and method of the present invention for evaporating the gas, thereby securing the safety of the tank and the vessel, and improving the transportation efficiency of the LNG. In addition, the BOG is compressed using the energy generated when the refrigerant is thermally expanded, and the BOG is cooled with the refrigerant cooled through the thermal expansion, thereby realizing a compact and highly efficient system.

Fig. 1 schematically shows a partial redistribution device capable of treating an evaporative gas according to the applicant's prior patent.
2 schematically shows a vaporization gas remelting system according to a first embodiment of the present invention.
3 schematically shows a vaporization gas remelting system according to a second embodiment of the present invention.
4 schematically shows a vaporization gas remelting system according to a third embodiment of the present invention.
Fig. 5 schematically shows a modification of the evaporative gas remelting system of the third embodiment of the present invention.
Fig. 6 schematically shows a vaporized gas remelting system according to a fourth embodiment of the present invention.
FIG. 7 schematically shows a vaporization gas remelting system according to a fifth embodiment of the present invention.
8 schematically shows a vaporization gas remelting system according to a sixth 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.

First, the evaporation gas re-liquefaction systems to be described later of the present invention can be applied to all types of vessels and marine structures, namely LNG carriers, Liquefied Ethane Gas (LEG) carriers, LNG RVs And for marine structures such as LNG FPSO, LNG FSRU, and so on.

In the following embodiments, LNG, which is a representative low-temperature liquid cargo, is described as an example for convenience of explanation, but the present invention is not limited thereto. Liquefaction gas stored in such a storage tank may be any liquid cargo that can be transported by liquefying at a low temperature . For example, in addition to LNG, LEG, LPG, liquefied nitrogen, liquefied gas such as ethylene, acetylene, propylene, and the like may be applicable. These embodiments can be applied to the treatment of the evaporative gas generated from such liquefied gas.

FIG. 2 schematically shows a vaporization gas re-liquefaction system according to a first embodiment of the present invention.

As shown in FIG. 2, the system of the first embodiment includes a BOG re-liquefaction line RLa for compressing and cooling BOG (Boil-Off Gas) generated in an LNG storage tank provided in a ship or an offshore structure to re- And a refrigerant circulation line (CLa) through which the refrigerant for cooling the BOG circulates.

A compander 100a for compressing BOG is provided in the BOG re-liquefaction line RLa. The compander includes an expander 101a for receiving and expanding the refrigerant and expanding the refrigerant in the expander 101a, And a BOG compressor 102a for compressing BOG. In the compander 100a, the refrigerant is cooled by the thermal expansion at the side of the expander 101a while compressing the BOG at the side of the compressor 102a by using the expansion force when the refrigerant in the expander is thermally expanded. In the compander, the expander can be provided, for example, as a turbine type. The expansion force obtained when the refrigerant is thermally expanded in the expander is transferred to the compressor connected to the expander through the kinetic energy when the turbine is rotated. The BOG can be compressed.

The BOG liquefaction line (RLa) is further provided with a booster compressor (110a) which receives the BOG compressed by the BOG compressor (102a) and further compresses the BOG.

In the BOG compressor 102a of the compander 100a, the BOG is compressed to a pressure of about 3 to 10 bar and is further compressed through the booster compressor 110a to increase the re-liquefaction efficiency of the BOG, . The BOG compressed by the compander's BOG compressor branches off before it is introduced into the booster compressor 110a when the supply pressure of the fuel required by the low pressure fuel consuming place (not shown) provided on the ship or offshore structure is such that It can also be supplied as a low-pressure fuel consuming place. The low-pressure fuel consumer may be, for example, a ship's power generation engine, more specifically a DFDE.

The BOG re-liquefaction line RLa is further provided with a main heat exchanger 120a for cooling the BOG compressed by the BOG compressor 102a and the booster compressor 110a by heat exchange with the refrigerant which is thermally expanded in the expander 101a, A flash drum 140a that receives BOG or LNG reduced in pressure by the BOG or the main heat exchanger cooled by the heat exchanger and receives the LNG generated from the BOG to reduce the pressure thereof; .

The decompression means 130a may be, for example, an expansion valve (J-T valve) or an expander, and may be decompressed to atmospheric pressure while passing through the decompression means. During the decompression process, the BOG or LNG is further cooled and enters the flash drum. In the flash drum 140a, the LNG re-liquefied through gas-liquid separation is restored to the LNG storage tank. The non-re-liquefied gas or the flash gas generated in the flash drum can be supplied upstream of the BOG re-liquefaction line (RLa) for re-liquefaction or as fuel in the ship. Alternatively, they can be processed or vented in the GCU.

That is, the BOG compressed by the BOG compressor 102a of the compander 100a and the booster compressor 110a at a pressure equal to or higher than the critical pressure is mono-expanded in the main heat exchanger 120a through the expander 101a of the compander, Cooled by heat exchange with the cooled refrigerant. The critical pressure of methane, which forms the majority of the BOG, is about 55 bar. After passing through the BOG compressor and the booster compressor, it is compressed to a pressure higher than the critical pressure to 70 bar and then introduced into the main heat exchanger. When the BOG is introduced into the main heat exchanger while being compressed to a high pressure of about the critical pressure, it can be re-liquefied by effecting phase change through heat exchange with the refrigerant. The BOG cooled at a low temperature of about -150 deg. C through the main heat exchanger 120a is decompressed and further cooled through the thermal expansion via the decompression means 130a such as an expansion valve (JT valve) or an expander, (140a). In the flash drum, the liquefied LNG from the BOG is separated from the gaseous flash gas, and the LNG is restored to the LNG storage tank.

On the other hand, the refrigerant circulation line (CLa) includes a refrigerant compressor (200a) for receiving and compressing the refrigerant discharged from the main heat exchanger after heat exchange with the BOG, a refrigerant precooler (210a) for cooling the refrigerant and supplying it to the expander, . In the refrigerant precooler 210a, the refrigerant compressed by the refrigerant compressor can be cooled by the heat exchange with the refrigerant before being compressed to be introduced into the refrigerant compressor, and then supplied to the expander 101a. By providing a refrigerant compressor with a large duty and providing a refrigerant precooler, only a single compander is provided in the BOG re-liquefaction line to obtain a refrigerant at a low temperature sufficient to re-liquefy BOG even if only one expander is loaded with refrigerant , The configuration of the system can be simplified.

Coolers 105a, 115a, and 205a are provided at the rear ends of the respective compressors, such as the compander BOG compressor, the booster compressor of the BOG re-liquefaction line, and the refrigerant compressor. For example, in the cooler 205a at the downstream of the refrigerant compressor 200a, the refrigerant can be primarily cooled to room temperature around 25 ° C through heat exchange with fresh water. The refrigerant cooled in the cooler at the downstream of the compressor is introduced into the refrigerant precooler and further cooled through heat exchange with the refrigerant before compression.

The BOG generated from the LNG storage tank may also be configured to pass through the refrigerant precooler 210a before being introduced into the BOG compressor 102a. Since LNG in the LNG storage tank is cryogenic at around -160 ° C, BOG generated from the LNG storage tank is also low in temperature and can be an effective cold / heat source when introduced into a refrigerant precooler.

The refrigerant is further cooled by the refrigerant precooler 210a to a low temperature of -10 ° C or lower, preferably -30 ° C or lower, through heat exchange with the refrigerant before compression, BOG from the LNG storage tank to be introduced into the BOG compressor of the compander, And then supplied to the expander 101a of the compander. In this case, however, it is preferable that the temperature of the refrigerant can be maintained above the critical temperature in order to prevent a device malfunction that may occur when the liquid refrigerant is supplied to the expander. The refrigerant is further cooled while being thermally expanded in the expander of the compander, and introduced into the main heat exchanger.

As the refrigerant circulating in the refrigerant circulation line CLa, BOG, nitrogen (N 2 ) may be used, or a mixed refrigerant containing methane and nitrogen may be used. The composition of the refrigerant can be freely configured.

FIG. 3 schematically shows a vaporization gas re-liquefaction system according to a second embodiment of the present invention.

As shown in FIG. 3, the system of the second embodiment compresses and cools BOG (Boil-Off Gas) generated in the LNG storage tank provided in a ship or a marine structure, as in the first embodiment, And a refrigerant circulation line (CLb) through which a refrigerant for cooling the BOG circulates.

The BOG liquefaction line also includes a compander 100b including an expander 101b for receiving and expanding the refrigerant and a BOG compressor 101b for compressing the BOG using the expanding force of the refrigerant in the expander, A main heat exchanger 120b for cooling the compressed BOG by heat exchange with the refrigerant that is thermally expanded in the expander, and a booster compressor 110b for supplying the compressed BOG from the BOG compressor to the main heat exchanger by further compressing the BOG .

In this embodiment, the fuel supply line FLb branched from the BOG re-liquefaction line is provided so that the compressed BOG from the downstream of the compander can be supplied as fuel to the in-line high-pressure gas consuming place. The BOG branched after the compression through the fuel supply line FLb is mixed with the LNG supplied from the LNG storage tank, recycled, compressed and forcedly vaporized, and supplied as fuel for the high pressure gas consuming place.

As in the embodiment described above, the refrigerant circulation line CLb also includes a refrigerant compressor 200b for receiving and compressing BOG from the main heat exchanger and the refrigerant discharged after heat exchange, and refrigerant compressed by the refrigerant compressor And a refrigerant precooler 210b for cooling and supplying the refrigerant to the expander is provided.

In the refrigerant precooler 210b, uncompressed refrigerant to be introduced into the refrigerant compressor, BOG to be generated from the LNG storage tank and supplied to the BOG compressor, LNG recondensed and compressed in the fuel supply line, and BOG It is possible to cool the refrigerant through heat exchange by receiving a flash gas generated during re-condensation of the refrigerant. If the amount of BOG to be re-liquefied is large, the refrigerant can be cooled from the LOG by heat exchange if the amount of compressed LNG to be supplied from the BOG is large. If the amount of LNG to be supplied to the BOG or the fuel is small It is possible to cool the refrigerant by circulating the refrigerant under any condition, and to re-liquefy the BOG.

The BOG re-liquefaction line RLb is provided with a decompression means 130b for decompressing the LNG generated from the BOG or BOG cooled by the main heat exchanger, a flash drum 130 for receiving the BOG or LNG decompressed by the decompression means, 140b.

Compressor BOG compressors, on the other hand, can also be supplied as fuel to low pressure fuel consuming areas on ships or offshore structures.

The fuel supply line FLb includes a recondensor 300b which receives BOG branched from the front end or the rear end of the booster compressor and mixes LNG supplied from the LNG storage tank to cool the LNG, A high pressure pump 310b for compressing the gas at the supply pressure of the gas consuming place and a vaporizer 320b for forcibly vaporizing the LNG compressed in the high pressure pump may be provided. LNG can be supplied to the LNG storage tank by a feed pump (Pb) provided in an in tank type.

The high-pressure gas consumer (not shown) may be, for example, a propulsion engine or a power generation engine for a ship or the like, and more specific examples may include ME-GI engine, DF generator, gas turbine, DFDE and the like. The high pressure gas is supplied according to the fuel supply condition of the gas consuming place. For example, if the gas consuming place is the ME-GI engine, high pressure gas of about 150 to 400 bar, more preferably 300 bar can be supplied. For example, if the ME-GI engine is used as a propulsion engine for a ship, the high-pressure pump compresses the LNG supplied from the condenser to a supercritical pressure of about 300 bar, and then, through a vaporizer, And can be supplied as fuel. However, since the gas and liquid can not be distinguished from each other in the supercritical state, the expression 'forced LNG is vaporized' means that the compressed LNG is supplied with thermal energy to raise the temperature (or, in a denser supercritical state, Critical state) may be meaningful.

A fuel heating line HLb branched from the fuel supply line FLb at the rear end of the high pressure pump 310b and connected to the fuel supply line at the front end of the vaporizer 320b via the refrigerant precooler 210b is provided. The low-temperature LNG compressed through the high-pressure pump is supplied to the front end of the vaporizer while being supplied with thermal energy from the refrigerant while cooling the compressed refrigerant while passing through the refrigerant precooler. By constituting the fuel heating line HLb through the refrigerant precooler in this way, the refrigerant in the refrigerant circulation line CLb can be effectively cooled, and at the same time, the high-pressure LNG to be supplied as fuel to the high-pressure gas consumption point can be effectively heated , The load on the carburetor can be reduced.

Meanwhile, in the re-condenser 300b, the flash gas generated when the BOG and the LNG are mixed is supplied to the upstream side of the compander 100b of the BOG re-liquefaction line RLb through the flash gas supply line GLb to re-liquefy .

The refrigerant circulating in the refrigerant circulation line CLb may be, for example, a mixed refrigerant containing BOG, nitrogen (N 2 ), and methane, and may be used to prevent an apparatus malfunction that may occur when a liquid refrigerant is supplied to the expander , So that the temperature of the refrigerant can be maintained above the critical temperature. Accordingly, the flow rate of the BOG, the compressed LNG, etc., which is introduced into the refrigerant precooler 210b and exchanges heat with the refrigerant, is controlled according to the refrigerant so that the refrigerant supplied to the expander can maintain the temperature above the critical temperature.

The description overlapping with the first embodiment described above will be omitted.

Next, FIG. 4 schematically shows a vaporization gas remelting system according to a third embodiment of the present invention.

As shown in FIG. 4, the system of the third embodiment also includes a BOG (Boil-Off Gas) system for compressing and cooling BOG (Boil-Off Gas) generated in an LNG storage tank provided in a ship or a marine structure, A re-liquefaction line RLc, and a refrigerant circulation line CLc through which the refrigerant for cooling the BOG circulates.

A compander 100c is also provided in the BOG re-liquefaction line of the present embodiment. The compander of the present embodiment includes an expander 101c for receiving and expanding the refrigerant to expand and expand the refrigerant, an expander 101c connected to the expander, A motor 103c, and a BOG compressor 102c that is connected to the rotation shaft of the motor and compresses the BOG by the rotational force. The BOG compressor can sufficiently compress BOG at a constant pressure by the motor 103c so that the booster compressor as in the first and second embodiments described above can be omitted and the system configuration can be simplified.

The BOG compressed through the BOG compressor 102c is re-liquefied while being cooled through heat exchange with the refrigerant which is mono-thermally expanded via the expander in the main heat exchanger 120c.

The refrigerant circulation line CLc is provided with a refrigerant compressor 200c for receiving and compressing the BOG and the refrigerant discharged after heat exchange from the main heat exchanger in the same manner as in the above embodiment and a refrigerant compressor 200c for cooling the refrigerant compressed by the refrigerant compressor, And a refrigerant precooler 210c is provided.

The refrigerant in the refrigerant precooler 210c can be cooled by heat exchange with the BOG to be supplied to the BOG compressor from the LNG storage tank and the uncompressed refrigerant to be introduced into the refrigerant compressor as in the above- And may be configured to cool the refrigerant compressed through heat exchange.

The BOG generated from the LNG storage tank is supplied to the refrigerant precooler 210c, is heat-exchanged with the compressed refrigerant, is supplied to the BOG compressor 102c, is compressed through the BOG compressor, Lt; / RTI > The LNG generated from the BOG and the cooled BOG generated through the cooling are decompressed through the decompression means 130c and then separated from the flash drum 140c. The LNG is supplied to and stored in the LNG storage tank.

The refrigerant circulating in the refrigerant circulation line CLc may be BOG, nitrogen (N 2 ), mixed refrigerant containing methane, or the like as in the above-described embodiments.

Fig. 5 schematically shows a system of a modification of the evaporative gas remelting system of the third embodiment described above.

5, the compressed BOG is branched from the downstream side of the BOG compressor 102c " of the compander 100c " in the BOG liquefaction line RLc " A system configured to mix the branched compressed BOG with the LNG supplied from the LNG storage tank and re-condense the compressed BOG, and to compress and force-vaporize the compressed LNG to supply the high pressure gas consuming place as fuel to be. The supply of fuel to the in-line high-pressure gas consuming place has been described in the system of the second embodiment described above, so duplicate description is omitted.

FIG. 6 schematically shows a vaporization gas re-liquefaction system according to a fourth embodiment of the present invention.

As shown in FIG. 6, the system of the fourth embodiment also includes a BOG re-liquefaction line RLd for compressing and cooling the BOG (Boil-Off Gas) generated in the LNG storage tank and re- And a refrigerant circulation line (CLd) through which the refrigerant for cooling the BOG circulates.

Like the system of the third embodiment described above, in the present embodiment, the compander 100d provided in the BOG liquefaction line is provided with an expander 101d for receiving and expanding the refrigerant to expand the refrigerant, an expander 101d connected to the expander, And a BOG compressor 102d that is connected to the rotation shaft of the motor and compresses the BOG by a rotational force.

As in the modified example of the third embodiment described above, the fourth embodiment also divides the compressed BOG from the downstream of the compander 100d in the BOG liquefaction line (RLd) and mixes it with the LNG supplied from the LNG storage tank A fuel supply line FLd is provided for recondensing, compressing, and forcedly vaporizing and supplying fuel as a fuel of a high-pressure gas consumption source.

The refrigerant circulation line CLd is provided with a refrigerant compressor 200d for receiving and compressing the BOG and the refrigerant discharged after heat exchange from the main heat exchanger in the same manner as in the above-described embodiments, and the refrigerant compressed by the refrigerant compressor, A refrigerant precooler 210d is provided. In the refrigerant precooler, heat exchange between the BOG to be supplied to the BOG compressor from the LNG storage tank, the recondensed and compressed LNG from the fuel supply line, and the flash gas generated during the recondensing of the BOG in the fuel supply line Thereby cooling the refrigerant. In this embodiment as in the above-described embodiment, the cold of the uncompressed refrigerant to be introduced into the refrigerant compressor can also be used for cooling the refrigerant compressed in the refrigerant precooler.

The fuel supply line FLd includes a recondensor 300d which receives BOG branched from the downstream of the compander and mixes LNG supplied from the LNG storage tank to cool the LNG, A high pressure pump 310d for compressing at a supply pressure and a vaporizer 320d for forcibly vaporizing the LNG compressed at the high pressure pump are provided. The LNG containing the LNG recycled from the BOG in the condenser is supplied to the high pressure pump 310d and the flash gas generated when the BOG and the LNG are mixed is supplied to the BOG re-liquefaction line RLd).

At this time, the system of this embodiment further includes a BOG expander 330d in the fuel supply line to cool the BOG branched from the downstream of the compander to the monotonic expansion through the BOG expander 330d, ). This branched BOG can be recycled more efficiently in the re-condenser by being thermally expanded and cooled by isentropic motion before being introduced into the re-condenser through the BOG expander in the fuel supply line. Other devices such as other expansion valves may be configured to replace the BOG expander.

The LNG compressed in the high pressure pump is heated while exchanging heat with the refrigerant through the refrigerant precooler 210d through the fuel heating line HLd branched from the fuel supply line FLd at the rear end of the high pressure pump 310d to be supplied to the evaporator 320d .

On the other hand, in the system of this embodiment, a liquid expander 150d is further provided upstream of the decompression means 130d in the BOG liquefaction line RLd, and the BOG or LNG cooled in the main heat exchanger is expanded and decompressed And supplied to the decompression means. The liquid refluxing efficiency of the BOG can be further increased by decompressing and cooling the liquid expander 150d and the decompression means 130d repeatedly.

The BOG or LNG, which is decompressed via the liquid expander and the decompression means, is supplied to a flash drum (140d) to be gas-liquid separated, and the LNG re-liquefied from the BOG is restored to the LNG storage tank.

The description overlapping with the above embodiments is omitted.

FIG. 7 schematically shows a vaporization gas remelting system according to a fifth embodiment of the present invention.

As shown in FIG. 7, the system of the fifth embodiment also includes a BOG re-liquefaction line (RLe) for compressing and cooling BOG (Boil-Off Gas) generated in the LNG storage tank to re- And a refrigerant circulation line (CLe) through which the refrigerant circulates.

The BOG re-liquefaction line (RLe) is provided with an expander (101e) for receiving and expanding the refrigerant and for thermally expanding the refrigerant, and a BOG compressor (102e) for compressing the BOG using the expanding force of the refrigerant in the expander and the BOG compressed by the BOG compressor is cooled by heat exchange with the refrigerant which is swollen by the expander from the main heat exchanger 120e.

The system of the present embodiment is advantageous in that the BOG compressed in the BOG compressor 102e is cooled in the main heat exchanger 120e by the refrigerant cooled from the expander to the thermal expansion without further compression through the device such as the booster compressor configured in the above- And can be liquefied by heat exchange with the liquid.

For this purpose, the refrigerant circulating in the refrigerant circulation line CLe in this embodiment uses a nitrogen (N 2 ) refrigerant or a mixed refrigerant containing nitrogen (N 2 ) of 50% or more.

If the refrigerant in the refrigerant circulation line CLe is maintained to contain nitrogen of 50% or more, the temperature of the refrigerant can be sufficiently lowered, so that the compressed BOG or the BOG close to the normal pressure is cooled through only the BOG compressor of the compander 100e The liquid can be re-liquefied. By using such a refrigerant, there is no need to construct a booster compressor as in the above-described embodiment, so that it is possible to reduce the number of apparatuses and reduce the installation cost, thereby realizing an economical and compact system.

The refrigerant circulation line CLe is provided with the refrigerant compressor 200e and the refrigerant precooler 210e in the refrigerant circulation line CLe and the uncompressed refrigerant to be introduced into the refrigerant compressor for cooling the refrigerant in the refrigerant pre- , BOG to be supplied from the LNG storage tank to the BOG compressor may be used. The LNG compressed through the high pressure pump 310e may be introduced into the vaporizer 320e through the refrigerant precooler 210e and heated while supplying fuel to the high pressure gas consuming place in the ship.

LNG generated from the BOG or BOG cooled through the heat exchange with the refrigerant in the main heat exchanger 120e is decompressed through the decompression means 130e and is separated from the gas via the flash drum 140e.

In order to more effectively re-liquefy the BOG, it is also possible to provide a liquid expander (not shown) upstream of the decompression means in the BOG re-liquefaction line as in the fourth embodiment described above.

It is also possible to provide a compander including a motor which is connected to the expander and which converts the expansion force of the refrigerant to the rotational force as in the third embodiment described above.

The description overlapping with the above embodiments is omitted.

FIG. 8 schematically shows a vaporization gas remelting system according to a sixth embodiment of the present invention.

As shown in FIG. 8, the system of the sixth embodiment is also similar to the above-described embodiments in that the BOG material for re-liquefying the BOG (Boil-Off Gas) generated in the LNG storage tank of a ship or a marine structure, A refrigerant circulation line CLf in which a refrigerant for cooling the BOG is circulated and a BOG compressed from the downstream of the compander in the BOG re-liquefaction line are branched and mixed with the LNG supplied from the LNG storage tank And a fuel supply line (FLf) for re-condensing, compressing, and forcedly vaporizing and supplying the fuel to the high-pressure gas consuming place.

The BOG re-liquefaction line (RLf) is provided with an expander (101f) for receiving and expanding the refrigerant and performing a thermal expansion, and a BOG compressor (102f) for compressing the BOG using the expanding force of the refrigerant in the expander and the BOG compressed by the BOG compressor of the compander is cooled by heat exchange with the refrigerant which is swelled in the main heat exchanger 120f through the expander.

As in the fifth embodiment described above, the BOG compressed by the BOG compressor of the compander is supplied to the main heat exchanger 120f without further compression, and is liquefied by heat exchange with the refrigerant cooled by the expansion in the expander A nitrogen (N 2 ) refrigerant or a mixed refrigerant containing 50% or more nitrogen (N 2 ) is used as a refrigerant.

The refrigerant circulation line (CLf) includes a refrigerant compressor (200f) that receives and compresses the refrigerant discharged from the main heat exchanger after heat exchange with the BOG, a refrigerant precooler that cools the refrigerant compressed by the refrigerant compressor and supplies it to the expander, (210f).

In the refrigerant precooler, uncompressed refrigerant to be introduced into the refrigerant compressor, BOG generated from the LNG storage tank and supplied to the BOG compressor, re-condensed and compressed LNG in the fuel supply line, It is possible to cool the refrigerant through heat exchange with a flash gas or the like. If the amount of BOG to be re-liquefied is large, the refrigerant can be cooled from the LOG by heat exchange if the amount of compressed LNG to be supplied from the BOG is large. If the amount of LNG to be supplied to the BOG or the fuel is small It is possible to cool the refrigerant by circulating the refrigerant under any condition, and to re-liquefy the BOG.

LNG generated from the BOG or BOG cooled in the main heat exchanger 120f is decompressed through the decompression means 130f and gas-liquid separated from the flash drum 140f, and the re-liquefied LNG is transferred to the LNG storage tank . The gas in the gaseous state separated from the flash drum can be introduced through the gas re-liquefaction line (GRLf) upstream of the compander (100f) of the BOG re-liquefaction line (RLf).

In the fuel supply line FLf, the BOG branched from the downstream of the compander is supplied to the re-condenser, and the LNG supplied from the LNG storage tank is mixed and cooled. In the high-pressure pump 310f supplied with LNG from the re- The gas is compressed by the supply pressure of the consuming place. The LNG compressed in the high-pressure pump is forcedly vaporized in the vaporizer 320f and supplied as fuel to the high-pressure gas consuming place. The compressed LNG may be branched from the fuel supply line at the rear end of the high pressure pump, heated by supplying heat energy from the refrigerant through the fuel heating line HLf through the refrigerant precooler, and then supplied to the front end of the vaporizer 320f .

Also in this embodiment, as in the fourth embodiment, a BOG expander (not shown) for cooling the BOG branched from the downstream of the compander to a single condenser so as to effectively recycle the BOG in the re- Not shown) may be provided in the fuel supply line.

The description overlapping with the above-described embodiment is omitted.

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 and scope of the invention. It is.

RLa, RLb, RLc, RLd, RLe, RLf: The BOG liquefaction line
CLa, CLb, CLc, CLd, CLe, CLf: refrigerant circulation line
100a, 100b, 100c, 100d, 100e, 100f:
120a, 120b, 120c, 120d, 120e, 120f: main heat exchanger
130a, 130b, 130c, 130d, 130e, and 130f:
140a, 140b, 140c, 140d, 140e, 140f:
200a, 200b, 200c, 200d, 200e, 200f: refrigerant compressor
210a, 210b, 210c, 210d, 210e, 210f: a refrigerant precooler

Claims (10)

A BOG re-liquefaction line for compressing and cooling BOG (Boil-Off Gas) generated in an LNG storage tank provided in a ship or a marine structure to re-liquefy the same;
A refrigerant circulation line through which the refrigerant for cooling the BOG circulates;
A compander provided in the BOG re-liquefaction line and including an expander for receiving and expanding the refrigerant, and a BOG compressor for compressing the BOG using the expansion force of the refrigerant in the expander;
A main heat exchanger for cooling the compressed BOG by heat exchange with the refrigerant which is thermally expanded in the expander;
A booster compressor provided in the BOG re-liquefaction line for supplying the compressed BOG from the BOG compressor to the main heat exchanger;
A fuel supply line for branching the compressed BOG from the downstream of the compander in the BOG re-liquefaction line, mixing the re-condensed LNG with the LNG supplied from the LNG storage tank, and compressing and supplying the compressed BN to the high-
A refrigerant compressor provided in the refrigerant circulation line for receiving and compressing the refrigerant discharged from the main heat exchanger after heat exchange with the BOG;
A refrigerant precooler provided in the refrigerant circulation line for cooling the refrigerant compressed by the refrigerant compressor and supplying the refrigerant to the expander;
A recondenser provided in the fuel supply line and supplied with the BOG branched from the front end or the rear end of the booster compressor to mix and cool the LNG supplied from the LNG storage tank;
A high pressure pump which is provided in the fuel supply line and receives LNG from the re-condenser and compresses the LNG at a supply pressure of the high pressure gas consuming place;
A carburetor provided in the fuel supply line for forcibly vaporizing the LNG compressed by the high-pressure pump;
A fuel heating line branched from the fuel supply line at a rear end of the high-pressure pump and connected to the fuel supply line from the front end of the vaporizer via the refrigerant precooler; And
And a flash gas supply line for supplying a flash gas generated when the BOG and LNG are mixed in the re-condenser to the upstream of the compander of the BOG re-liquefaction line,
The BOG being generated from the LNG storage tank and supplied to the BOG compressor, the LNG recondensed and compressed in the fuel supply line, and the LNG compressed in the fuel supply line, Exchanges heat with at least one of flash gas generated during recondensing of the BOG in the line to cool the refrigerant. delete delete The method according to claim 1,
Decompression means provided in the BOG liquefaction line and depressurizing the BOG cooled in the main heat exchanger or the LNG generated from the BOG; And
Further comprising a flash drum provided in the BOG re-liquefaction line, the flash drum being supplied with the BOG or LNG decompressed by the decompression means and performing gas-liquid separation. The method according to claim 1,
Wherein the BOG compressed by the BOG compressor of the compander can be supplied as fuel to a low-pressure fuel consuming place provided in the ship or the offshore structure. delete delete The method according to claim 1,
Wherein the refrigerant circulating through the refrigerant circulation line is BOG, nitrogen (N2), or a mixed refrigerant containing methane and nitrogen. delete delete
KR1020150060310A 2015-04-29 2015-04-29 Boil Off Gas Reliquefaction System And Method KR101739986B1 (en)

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Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101356003B1 (en) * 2012-10-24 2014-02-05 대우조선해양 주식회사 System for treating boil-off gas for a ship

Patent Citations (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR101356003B1 (en) * 2012-10-24 2014-02-05 대우조선해양 주식회사 System for treating boil-off gas for a ship

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