KR101765385B1 - A Treatment System of Liquefied Gas - Google Patents

A Treatment System of Liquefied Gas Download PDF

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Publication number
KR101765385B1
KR101765385B1 KR1020150058965A KR20150058965A KR101765385B1 KR 101765385 B1 KR101765385 B1 KR 101765385B1 KR 1020150058965 A KR1020150058965 A KR 1020150058965A KR 20150058965 A KR20150058965 A KR 20150058965A KR 101765385 B1 KR101765385 B1 KR 101765385B1
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KR
South Korea
Prior art keywords
liquefied gas
gas
cooler
liquefied
refrigerant
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KR1020150058965A
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Korean (ko)
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KR20160127880A (en
Inventor
한주석
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현대중공업 주식회사
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Priority to KR1020150058965A priority Critical patent/KR101765385B1/en
Publication of KR20160127880A publication Critical patent/KR20160127880A/en
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Publication of KR101765385B1 publication Critical patent/KR101765385B1/en

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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
    • 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

Abstract

The present invention relates to a liquefied gas processing system, comprising: a pump for pressurizing liquefied gas discharged from a liquefied gas storage tank; A heat exchanger for heating the pressurized liquefied gas; A cooler for heat-exchanging the pressurized or heated liquefied gas with the refrigerant; And a liquefier for liquefying or expanding the liquefied gas cooled in the cooler to at least partially liquefy the liquefied gas.
The liquefied gas processing system according to the present invention is characterized in that a liquefied gas discharged from a liquefied gas storage tank is pressurized and heated by a pump and a heat exchanger and then at least partially liquefied through cooling using a refrigerant such as nitrogen and decompression or expansion, By returning to the storage tank, the liquefied gas can be recycled.

Description

Description of the Related Art A Treatment System of Liquefied Gas

The present invention relates to a liquefied gas processing system.

A ship is a means of transporting large quantities of minerals, crude oil, natural gas, or more than a thousand containers. It is made of steel and buoyant to float on the water surface. ≪ / RTI >

Such a vessel generates thrust by driving the engine. In this case, the engine uses gasoline or diesel to move the piston so that the crankshaft is rotated by the reciprocating motion of the piston, so that the shaft connected to the crankshaft is rotated to drive the propeller It was common.

In recent years, however, LNG fuel supply systems for driving an engine using LNG as a fuel have been used in an LNG carrier carrying Liquefied Natural Gas (LNG) It is also applied to other ships.

Generally, it is known that LNG is a clean fuel and its reserves are more abundant than petroleum, and its usage is rapidly increasing as mining and transfer technology develops. This LNG is generally stored in a liquid state at a temperature of -162 ° C. or below under 1 atm. The volume of liquefied methane is about one sixth of the volume of methane in a gaseous state, The specific gravity is 0.42, which is about one half of that of crude oil.

However, the temperature and pressure required to drive the engine may be different from the state of the LNG stored in the tank. Therefore, in recent years, research and development have been made on the technology of controlling the temperature and pressure of the LNG stored in the liquid state and supplying the engine to the engine.

SUMMARY OF THE INVENTION The present invention has been made in order to solve the problems of the prior art as described above, and it is an object of the present invention to provide a liquefied natural gas which is pressurized and heated at a high pressure, then heat-exchanged with a refrigerant such as nitrogen, cooled, And to provide a liquefied gas processing system capable of realizing re-liquefaction with a simple configuration by liquefaction.

It is also an object of the present invention to provide a liquefied gas processing system capable of accurately calculating a re-liquefaction rate by sensing the level of liquefied gas liquefied by depressurization or expansion.

A liquefied gas processing system according to an aspect of the present invention includes a pump for pressurizing liquefied gas discharged from a liquefied gas storage tank; A heat exchanger for heating the pressurized liquefied gas; A cooler for heat-exchanging the pressurized or heated liquefied gas with the refrigerant; And a liquefier for liquefying or expanding the liquefied gas cooled in the cooler to at least partially liquefy the liquefied gas.

Specifically, the system may further include a liquefied gas supply line connected from the liquefied gas storage tank to a customer, and the pump and the heat exchanger may be provided in the liquefied gas supply line.

Specifically, a liquefied gas cooling line branched from the liquefied gas supply line and connected to the liquefied gas storage tank may be provided, and the cooler, the liquefier may be provided in the liquefied gas cooling line.

Specifically, it may further include a gas-liquid separator for separating the liquefied liquefied gas into a gas and a liquid.

Specifically, the gas-liquid separator can deliver a liquefied gas in a liquid state to the liquefied gas storage tank and deliver the liquefied gas in a gaseous state to the cooler.

Specifically, the cooler is capable of heat-exchanging the pressurized or heated liquefied gas with the gaseous liquefied gas delivered from the refrigerant and the gas-liquid separator.

Specifically, the heat exchanger changes the liquefied gas to a supercritical state of a critical pressure or higher and a critical pressure or higher, and the cooler performs heat exchange between the liquefied gas in the supercritical state and the refrigerant, , And the liquefier may change the supercooled liquefied gas to a liquid state at a critical temperature or lower and at a critical pressure or lower by depressurizing or expanding the liquefied gas.

The liquefied gas processing system according to the present invention is characterized in that a liquefied gas discharged from a liquefied gas storage tank is pressurized and heated by a pump and a heat exchanger and then at least partially liquefied through cooling using a refrigerant such as nitrogen and decompression or expansion, By returning to the storage tank, the liquefied gas can be recycled.

Further, the liquefied gas processing system according to the present invention can easily and accurately calculate the flow rate of the re-liquefied liquefied gas by sensing the level of the liquefied gas cooled by the refrigerant heat exchange and liquefied by the depressurization or expansion, thereby increasing the reliability of the system performance .

1 is a conceptual diagram of a liquefied gas processing system according to a first embodiment of the present invention.
2 is a conceptual diagram of a liquefied gas processing system according to a second embodiment of the present invention.
3 is a conceptual diagram of a liquefied gas processing system according to a third embodiment of the present invention.
4 is a conceptual diagram of a liquefied gas processing system according to a fourth embodiment of the present invention.
5 is a conceptual diagram of a liquefied gas processing system according to a fifth embodiment of the present invention.

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 liquefied gas processing system according to a first embodiment of the present invention.

1, a liquefied gas processing system 1 according to a first embodiment of the present invention includes a liquefied gas storage tank 10, a pump 20, a heat exchanger 30, a cooler 40, (50), a liquefier (60), and a gas-liquid separator (70).

Hereinafter, the liquefied gas means that the liquefied gas has been in a liquid state in the liquefied gas storage tank 10, and even if it changes to a liquid state, a supercooled state, a supercritical state, or even a gaseous state,

Hereinafter, the evaporation gas means that it is in a gaseous state in the liquefied gas storage tank 10, and the same can be said to be a vapor gas even if it changes to a gaseous state, a supercritical state, or even a liquid state.

The liquefied gas storage tank 10 stores liquefied gas. The liquefied gas stored in the liquefied gas storage tank 10 may be LNG, LPG, or the like, and at least most of the liquefied gas may be stored in a liquid state. At this time, the liquefied gas may be a liquefied gas to be supplied to the customer 2.

The customer 2 may be an engine configured to receive the liquefied gas and generate power. In this case, the engine may be an ME-GI engine manufactured by MAN DIESEL, or various known engines such as a DF engine.

Alternatively, the customer 2 may be a gas combustion unit (GCU), a boiler, a gas turbine, a city gas, or the like. In addition, the customer 2 may have various configurations consuming the liquefied gas, so the customer 2 in the present invention is not limited to the above example.

The liquefied gas storage tank 10 may be provided with a liquefied gas supply line 11 connected to the customer 2. The liquefied gas supply line 11 is provided with a pump 20 and a heat exchanger 30 . Further, a flow rate control valve (not shown), a pressure sensor (not shown), a flow rate sensor (not shown), and the like may be provided in the liquefied gas supply line 11.

The liquefied gas storage tank 10 may be manufactured in a heat insulating structure to store a fluid at a cryogenic temperature such as LNG, LPG, or the like. For example, when the liquefied gas is LNG, the liquefied gas storage tank 10 can maintain the internal temperature at -160 degrees centigrade or less.

To this end, the liquefied gas storage tank 10 may include an outer tank (not shown) and an inner tank (not shown), and an outer wall (not shown) provided between the outer tank and the inner tank.

The outer tank can be fixed to a structure such as a ship on which the present invention is installed, and the inner tank can be supported on the inner side of the outer tank by a support (not shown). At this time, the support can prevent the right and left and / or up-down movement of the tank.

The liquefied gas storage tank 10 including the outer tank, the inner tank, and the heat insulating wall may be a well-known independent tank, a membrane type tank, a pressure vessel type tank, and the like. 96 type or the like. It is needless to say that the present invention is not limited to the above-described configuration of the liquefied gas storage tank 10.

The pump 20 pressurizes the liquefied gas. Here, the liquefied gas may be a liquefied gas stored in the liquefied gas storage tank 10, or a liquefied gas discharged from the liquefied gas storage tank 10.

The pump 20 may include a booster pump 21 and a high-pressure pump 22. Both the booster pump 21 and the high-pressure pump 22 may be provided in the liquefied gas supply line 11 and may be provided in series to sequentially pressurize the liquefied gas.

The booster pump 21 may be provided inside the liquefied gas storage tank 10. Therefore, the booster pump 21 can maintain the cooled state and can discharge the liquefied gas stored in the liquefied gas storage tank 10 to the outside of the liquefied gas storage tank 10. [

The booster pump 21 can pressurize the liquefied gas at 1 to 12 bar, but the pressurized liquefied gas can still remain in the liquid state. The liquefied gas can be introduced into the high-pressure pump 22 in a liquid state.

The booster pump 21 may be a centrifugal pump, and as long as the liquefied gas is submerged in the liquefied gas storage tank 10, a cooldown may be omitted. Of course, in the present invention, the booster pump 21 may be provided outside the liquefied gas storage tank 10, unlike the case described above. In this case, it may be necessary to cool down the booster pump 21.

The high-pressure pump 22 pressurizes the liquefied gas delivered from the booster pump 21. The high pressure pump 22 may be a reciprocating pump having at least one cylinder (not shown) and a piston (not shown), and may pressurize the liquefied gas at 200 to 400 bar.

The liquefied gas pressurized by the high-pressure pump 22 may change to a supercooled state as the pressure exceeds the critical pressure. In this case, the liquefied gas can be raised only below the critical temperature even if the temperature is raised during the process of being pressurized by the high-pressure pump 22. [

On the other hand, when the liquefied gas is pressurized by the high-pressure pump 22 and the temperature rises to exceed the critical temperature, the liquefied gas changes into the supercritical state as the pressure and the temperature exceed the critical pressure and the critical temperature, can do. Supercritical state means a state in which the distinction between liquid and gas can not be made.

The high pressure pump 22 can pressurize the liquefied gas to a high pressure and deliver it to the heat exchanger 30. [ The temperature of the liquefied gas pressurized and heated by the high-pressure pump 22 may not reach the temperature required by the customer 2. Therefore, the present invention can heat the liquefied gas using the heat exchanger 30. [

The heat exchanger (30) heats the pressurized liquefied gas. The heat exchanger (30) may be provided on the liquefied gas supply line (11) downstream of the high-pressure pump (22). The heat exchanger 30 may be an electric heater using electricity, a heat exchanger 30 using glycol water mixed with ethylene glycol and water, a heat exchanger 30 using steam, or the like. That is, the manner in which the heat exchanger 30 heats the liquefied gas may be various, and the present invention does not limit the manner of the heat exchanger 30.

The heat exchanger 30 can heat the liquefied gas delivered by the high-pressure pump 22 to a temperature higher than the critical temperature because the temperature of the liquefied gas required by the customer 2 can be 20 to 40 degrees. When the liquefied gas delivered from the high-pressure pump 22 is in a subcooled state, the heat exchanger 30 can phase-change the liquefied gas to a supercritical state, while the liquefied gas delivered from the high- , The heat exchanger 30 can heat the liquefied gas while maintaining the liquefied gas in a supercritical state.

The cooler 40 heat-exchanges pressurized or heated liquefied gas with the refrigerant. The cooler 40 may be connected to the liquefied gas cooling line 41 which branches off from the liquefied gas supply line 11. [ At this time, the liquefied gas cooling line 41 may be connected to the downstream side of the heat exchanger 30. It should be understood that the liquefied gas cooling line 41 may be connected to the upstream of the heat exchanger 30 in the present invention.

The liquefied gas can be branched into the liquefied gas supply line 11 and the liquefied gas cooling line 41 downstream of the pump 20 or the heat exchanger 30 and a separate valve So that flow rate control can be performed.

The liquefied gas delivered to the liquefied gas supply line 11 is supplied to the customer 2 and the liquefied gas delivered to the liquefied gas cooling line 41 can be cooled by the cooler 40. However, the liquefied gas may flow into the liquefied gas supply line 11 and the liquefied gas cooling line 41, respectively, or may flow only to the liquefied gas supply line 11 or only to the liquefied gas cooling line 41 have.

In the liquefied gas cooling line 41, a flow meter 42 may be provided. The flow meter 42 measures the flow rate of the liquefied gas flowing along the liquefied gas supply line 11 and branched to the liquefied gas cooling line 41. The flow meter 42 is connected to the level sensor 73 of the gas- Can be used to estimate the efficiency.

That is, when the liquefied gas measured by the level sensor 73 of the gas-liquid separator 70 is regarded as a liquefied amount with the liquefied gas measured by the flow meter 42 as a total amount, calculation of the liquefied amount with respect to the total amount is simply possible Do.

Therefore, the present invention can easily and clearly show to what degree liquefied gas can be liquefied through the configuration of the cooler 40, the liquefier 60, and the like.

The cooler 40 cools the liquefied gas entering the liquefied gas cooling line 41 into the coolant after being pressurized by the pump 20 and / or heated by the heat exchanger 30. The refrigerant may be nitrogen or the like.

The cooler 40 can be supplied with a coolant such as nitrogen from a coolant tank 50 to be described later and the coolant tank 50 and the cooler 40 can be connected by a coolant line 51. The refrigerant line 51 is formed independently from the liquefied gas cooling line 41 to prevent mixing of the refrigerant and the liquefied gas, but is structured so as to efficiently perform heat exchange between the refrigerant and the liquefied gas in the cooler 40 .

The cooler 40 can cool the liquefied gas using the coolant, and at least a portion of the liquefied gas that has been cooled can be liquefied. However, the refrigerant transferred to the cooler 40 may be nitrogen in the gaseous state.

The cooler 40 can cool the liquefied gas supplied through the liquefied gas cooling line 41 using the gaseous liquefied gas delivered from the gas-liquid separator 70 to be described later together with the refrigerant. That is, in the cooler 40, the liquefied gas can be cooled by the refrigerant, the gaseous liquefied gas.

A gas transfer line 72 may be connected from the gas-liquid separator 70 to the cooler 40 and the gas transfer line 72 may be provided independently of the coolant line 51 and the liquefied gas cooling line 41 have. That is, the cooler 40 may be configured as a three stream structure that implements heat exchange between three independent lines.

The gas transfer line 72 can be joined to the refrigerant line 51. In this case, the gaseous liquefied gas delivered from the gas-liquid separator 70 is mixed with the refrigerant, Heat exchange with the liquefied gas of the heat exchanger 41 is possible. In this case, the cooler 40 may be configured as a two-stream structure in which the coolant line 51 and the liquefied gas cooling line 41 are independently provided.

The refrigerant tank (50) stores the refrigerant. In this case, the refrigerant may be nitrogen as mentioned above, and nitrogen may be stored in the refrigerant tank 50 in a liquid state.

The coolant tank 50 can deliver the stored nitrogen to the cooler 40 wherein the coolant can flow along the coolant line 51 connecting the coolant tank 50 and the cooler 40. The refrigerant that has passed through the cooler 40 may be vented to the outside or used by the customer 2 or various other consumers (not shown).

When the refrigerant is nitrogen, the coolant tank 50 can transfer nitrogen in the liquid state to the cooler 40, or can transfer nitrogen in the gaseous state to the cooler 40. The refrigerant tank 50 may be provided with a pressure build-up unit (PBU) in order to smoothly transfer the refrigerant to the cooler 40.

The PBU heats nitrogen in the liquid state in the refrigerant tank 50 and circulates the refrigerant to the refrigerant tank 50 so as to increase the internal pressure of the refrigerant tank 50 so that the refrigerant in the refrigerant tank 50 naturally flows along the refrigerant line 51 To the cooler (40).

The liquefier 60 decompresses or expands the cooled liquefied gas to at least partially liquefy it. The liquefier 60 may be a Joule-Thomson valve, which is a pressure reducing valve, or may be an inflator, and may be of various configurations that also reduce the pressure of the liquefied gas through depressurization or expansion.

As the liquefied gas in the cooler 40 is cooled by the coolant, it can be changed to a supercooled state below the critical temperature. At this time, the liquefier 60 may lower the pressure of the liquefied gas in the subcooled state to a critical pressure or lower, so that the liquefied gas changes to the liquid state.

The liquefier 60 can lower the pressure of the liquefied gas from 1 to 10 bar at 200 to 400 bar and at least a portion of the liquefied gas with reduced pressure can be liquefied.

The liquefier 60 is provided downstream of the cooler 40 in the liquefied gas cooling line 41 and downstream of the liquefier 60 a liquefied gas may be in a liquid state or a mixed state of liquid and gas.

The liquefied gas liquefied in the liquefier 60 may be supplied to the gas-liquid separator 70, which will be described later. If the liquefaction performance in the liquefier 60 can be sufficiently ensured, the gas-liquid separator 70 may be omitted.

The gas-liquid separator 70 separates the liquefied liquefied gas into gas and liquid. At this time, the gas-liquid separator 70 can deliver the liquefied gas in the liquid state to the liquefied gas storage tank 10. Thus, the liquefied gas cooled by the cooler 40 and liquefied by the liquefier 60 can be recovered to the liquefied gas storage tank 10 and reused.

A liquid recovery line 71 may be connected to the liquefied gas storage tank 10 in the gas-liquid separator 70 and the liquid recovery line 71 may be connected to the upper inside of the liquefied gas storage tank 10, The liquefied gas in the liquefied gas storage tank 10 can be supplied to the space where the evaporated gas is located. In this case, the liquefied gas in the liquid state cools the evaporated gas, thereby suppressing the generation of the evaporated gas.

Or the liquid recovery line 71 may be connected to the inner lower side of the liquefied gas storage tank 10 so that the liquid liquefied gas is recovered into the liquefied gas stored in the liquefied gas storage tank 10. [

While the gas-liquid separator 70 can deliver the gaseous liquefied gas to the cooler 40. The liquefied gas in the gaseous state transferred to the cooler 40 has a considerably low temperature since the cooler 40 and the liquefier 60 have already been roughened. Thus, the gaseous liquefied gas can cool the liquefied gas flowing into the cooler 40 along the liquefied gas cooling line 41.

A gas recovery line may be provided between the gas-liquid separator 70 and the cooler 40 so that the gaseous liquefied gas can be introduced from the gas-liquid separator 70 to the cooler 40. At this time, the gas recovery line can vent the gaseous liquefied gas heat exchanged in the cooler 40 to the outside.

The gas-liquid separator 70 is provided with a level sensor 73 and the level sensor 73 can measure the level (flow rate) of the liquid-state liquefied gas in the gas-liquid separator 70. The amount measured here means the amount of liquefied liquefied gas.

Therefore, when the amount of liquefied gas measured by the level sensor 73 is compared with the total amount of the liquefied gas measured by the flow meter 42, the present invention can be applied to the case where the liquefied gas passes through the cooler 40 and the liquefier 60 It is possible to easily grasp the performance of being liquefied.

As described above, in this embodiment, the efficiency of the liquefied gas to be liquefied can be accurately and simply tested while the liquefied gas is liquefied by the cooler 40 and the liquefier 60, so that reliability can be improved.

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

2, the liquefied gas processing system 1 according to the second embodiment of the present invention is characterized in that a refrigerant heat exchanger 52 can be added in comparison with the liquefied gas processing system 1 according to the first embodiment have. Other configurations are the same as or similar to those described in the first embodiment, and a detailed description thereof will be omitted.

The refrigerant heat exchanger (52) exchanges heat with the refrigerant. The refrigerant heat exchanger 52 may be provided between the refrigerant tank 50 and the cooler 40 in the refrigerant line 51. The refrigerant heat exchanger 52 may be provided between the refrigerant tank 50 and the cooler 40 and may cool the refrigerant or heat the refrigerant, Lt; / RTI >

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

3, the liquefied gas processing system 1 according to the third embodiment of the present invention is different from the liquefied gas processing system 1 according to the first embodiment in that the compressor 80, the evaporation gas supply line 81, and an evaporation gas heater 82 may be added. Other configurations are the same as or similar to those described in the first embodiment, and a detailed description thereof will be omitted.

The compressor (80) compresses the evaporation gas. The evaporation gas means a gas in a gaseous state generated by evaporation from the liquefied gas stored in the liquefied gas storage tank (10). In the liquefied gas storage tank 10, the evaporated gas may be discharged through the evaporated gas supply line 81 and transferred to the compressor 80.

The compressor (80) is capable of compressing the evaporation gas delivered through the evaporation gas supply line (81), but compressing the evaporation gas to at least one stage. For example, the compressor 80 may compress the evaporation gas in five stages, and the centrifugal compressor 80 and the reciprocating compressor 80 may be combined.

The compressor 80 is capable of compressing the evaporation gas of about 1 bar to a pressure of 200 to 400 bar by multi-stage compression. An intermediate cooler (not shown) is provided between the compressors 80 at each stage, It is possible to prevent the compression load from increasing as the volume increases.

The evaporation gas supply line 81 can supply the evaporation gas compressed by the compressor 80 to the customer 2. [ At this time, the evaporation gas supply line 81 may be joined to the liquefied gas supply line 11, and may be joined downstream of the heat exchanger 30 of the liquefied gas supply line 11, for example. In this case, the evaporation gas heater 82 may be used to match the temperature of the evaporated gas merged into the liquefied gas supply line 11 with the temperature of the liquefied gas downstream of the heat exchanger 30. [

Of course, when the evaporation gas supply line 81 is joined upstream of the heat exchanger 30 in the liquefied gas supply line 11, the evaporation gas and the liquefied gas are mixed and then heated integrally by the heat exchanger 30 The evaporation gas heater 82 can be omitted.

The evaporation gas heater 82 heats the compressed evaporation gas. The evaporation gas heater 82 can heat the evaporation gas to a temperature required by the consumer 2, and can heat the evaporation gas using a heating medium such as electricity or glycol water.

In this embodiment, in addition to the liquefied gas stored in the liquefied gas storage tank 10, the evaporation gas can be supplied to the customer 2. [ Therefore, the present embodiment can prevent the increase of the internal pressure as the evaporation gas is continuously generated in the liquefied gas storage tank 10, thereby increasing the possibility of breakage. Of course, in another embodiment in which there is no supply structure of the evaporative gas, a separate vent line (not shown) may be provided in the liquefied gas storage tank 10 to discharge the evaporated gas to the outside to increase the internal pressure of the liquefied gas storage tank 10 And it is needless to say that this embodiment may have a vent line together with the evaporation gas supply line 81.

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

4, the liquefied gas processing system 1 according to the fourth embodiment of the present invention is different from the liquefied gas processing system 1 according to the third embodiment in that the configuration of the gas delivery line 72 is different from that of the liquefied gas processing system 1 according to the third embodiment can do. Other configurations are the same as or similar to those described in the third embodiment, and a detailed description thereof will be omitted.

The gas transfer line 72 is connected to the cooler 40 in the gas-liquid separator 70 and can transfer the gaseous liquefied gas separated in the gas-liquid separator 70 to the cooler 40, May branch at a certain point, and may be connected to the evaporation gas supply line 81.

The gas delivery line 72 may be connected upstream of the compressor 80 in the evaporation gas supply line 81 and / or downstream of the compressor 80. The gas transfer line 72 may be configured to transfer the gaseous liquefied gas separated by the gas-liquid separator 70 to the evaporation gas supply line 81 to be supplied to the customer 2 or the cooler 40.

In the first to third embodiments, the gas transmission line 72 conveys the gaseous liquefied gas to the cooler 40, and ventilates the liquefied gas exiting the cooler 40. However, It is possible to reduce the amount of the external vent of the liquefied gas by connecting the liquefied gas that has escaped from the evaporator 40 or the liquefied gas that flows into the cooler 40 to the evaporation gas supply line 81.

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

5, the liquefied gas processing system 1 according to the fifth embodiment of the present invention is similar to the liquefied gas processing system 1 according to the third embodiment except that the cooler 40 and the gas transmission line 72 ) May be different. Other configurations are the same as or similar to those described in the third embodiment, and a detailed description thereof will be omitted.

The cooler 40 exchanges the liquefied gas introduced through the liquefied gas cooling line 41 with the refrigerant, and can also heat exchange the liquefied gas with the evaporated gas. That is, the cooler 40 can cool the liquefied gas to the coolant and the evaporated gas.

In this case, the cooler 40 may be a three-stream structure in which the liquefied gas cooling line 41, the refrigerant line 51, and the evaporation gas supply line 81 are independently flown. In this case, the gas delivery line 72 may be connected to the evaporation gas supply line 81 upstream of the cooler 40.

The evaporated gas and the gaseous liquefied gas separated by the gas-liquid separator 70 are transferred to the cooler 40 through the evaporation gas supply line 81 and the cooler 40 is introduced into the cooler 40 through the liquefied gas cooling line 41 And the cooled liquefied gas can be cooled with a refrigerant, an evaporating gas, or a liquefied gas in a gaseous state.

In this case, the flow rate of the liquid flowing into the cooler 40 through the liquefied gas cooling line 41 is measured by the flow meter 42, and the liquefied gas in the liquid state separated by the gas-liquid separator 70 is measured by the level sensor 73 The calculation of the re-liquefaction efficiency by the cooler 40 and the liquefier 60 can be performed simply and accurately as in the first embodiment.

In the present embodiment, the gaseous liquefied gas separated by the gas-liquid separator 70 is transferred to the customer 2 or the cooler 40 via the cooler 40 and the compressor 80, Can be recycled without venting to the outside.

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

6, the liquefied gas processing system 1 according to the sixth embodiment of the present invention is different from the liquefied gas processing system 1 according to the first embodiment in that the gas transmission line 72 is cooled by liquefied gas Line 41 as shown in Fig.

At this time, the cooler 40 has a two-stream structure, in which the liquefied gas in the liquefied gas cooling line 41 and the gaseous liquefied gas delivered from the gas-liquid separator 70 are mixed by the refrigerant line 51 It can be cooled by the supplied refrigerant. In this case, the gas delivery line 72 may be connected to the liquefied gas cooling line 41 upstream of the cooler 40 based on the liquefied gas flow of the liquefied gas cooling line 41, as shown in Fig.

Whereby the liquefied gas flowing along the liquefied gas cooling line 41 can be primarily cooled by the gaseous liquefied gas flowing along the gas transmission line 72 and then cooled secondarily by the cooler 40. [

Or the cooler 40 may be provided in a two stream structure and the liquefied gas in the liquefied gas cooling line 41 may be cooled by the coolant in the coolant line 51. [ In this case, the gas delivery line 72 may be connected to the liquefied gas cooling line 41 downstream of the cooler 40 based on the liquefied gas flow of the liquefied gas cooling line 41, as shown in FIG.

Thus, this embodiment can mix gaseous liquefied gas supplied through the gas delivery line 72 into the liquefied gas in the liquefied gas cooling line 41, either upstream or downstream of the cooler 40.

Alternatively, the present invention can be embodied as a combination of the embodiments of Figs. 1 and 6, such that the gas delivery line 72 can be joined to the liquefied gas cooling line 41 after passing through a three- have. The liquefied gas in the gaseous state flowing along the gas delivery line 72 at this time can be joined to the liquefied gas cooling line 41 after delivering cold heat to the liquefied gas in the liquefied gas cooling line 41 in the cooler 40.

The present invention can include both a new embodiment combining at least two embodiments and a new embodiment combining at least one embodiment and a known technology as well as the embodiments described above, The present invention is not limited thereto.

1: liquefied gas processing system 2: customer
10: liquefied gas storage tank 11: liquefied gas supply line
20: Pump 21: Booster pump
22: high-pressure pump 30: heat exchanger
40: cooler 41: liquefied gas cooling line
42: Flow meter 50: Refrigerant tank
51: Refrigerant line 52: Refrigerant heat exchanger
60: liquefier 70: gas-liquid separator
71: liquid recovery line 72: gas delivery line
73: Level sensor 80: Compressor
81: Evaporative gas supply line 82: Evaporative gas heater

Claims (7)

A pump for pressurizing the liquefied gas discharged from the liquefied gas storage tank;
A heat exchanger for heating the pressurized liquefied gas;
A cooler for heat-exchanging the pressurized or heated liquefied gas with the refrigerant;
A liquefier for decompressing or expanding the liquefied gas cooled in the cooler to at least partially liquefy the liquefied gas; And
And a gas-liquid separator for separating the liquefied liquefied gas into a gas and a liquid,
The gas-
Transferring the liquefied gas in a liquid state to the liquefied gas storage tank,
And transfers the gaseous liquefied gas to the cooler. The method according to claim 1,
Further comprising a liquefied gas supply line connected from the liquefied gas storage tank to a customer,
Wherein the pump and the heat exchanger are provided in the liquefied gas supply line. 3. The method of claim 2,
And a liquefied gas cooling line branched from the liquefied gas supply line and connected to the liquefied gas storage tank,
Wherein said cooler, said liquefier is provided in said liquefied gas cooling line. delete delete The apparatus of claim 1,
Wherein the pressurized or heated liquefied gas is heat-exchanged with the gaseous liquefied gas delivered from the refrigerant and the gas-liquid separator. The method according to claim 1,
Wherein the heat exchanger changes the liquefied gas from a critical temperature to a supercritical state at a critical pressure or more,
The cooler heat-exchanges the liquefied gas in the supercritical state with the refrigerant to change the supercooled state to a supercooled state below a critical temperature or above a critical pressure,
Wherein the liquefier changes the pressure of the liquefied gas in the supercooled state to a liquid state at a critical temperature or less and a critical pressure or less.


KR1020150058965A 2015-04-27 2015-04-27 A Treatment System of Liquefied Gas KR101765385B1 (en)

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JP2021517878A (en) * 2018-04-06 2021-07-29 コリア シップビルディング アンド オフショア エンジニアリング カンパニー リミテッド Gas treatment system and ships including it
KR102241203B1 (en) * 2019-02-01 2021-04-16 현대중공업 주식회사 Gas treatment system and ship having the same
WO2020159317A1 (en) * 2019-02-01 2020-08-06 현대중공업 주식회사 Gas processing system and ship including same
FR3093785B1 (en) * 2019-03-15 2021-06-04 Gaztransport Et Technigaz Pressure control system in a liquefied natural gas tank.

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KR101289212B1 (en) * 2013-05-30 2013-07-29 현대중공업 주식회사 A treatment system of liquefied gas
JP2014515072A (en) * 2011-03-22 2014-06-26 デウ シップビルディング アンド マリーン エンジニアリング カンパニー リミテッド Fuel supply system for high pressure natural gas injection engine with excess boil-off gas consumption means

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KR101289212B1 (en) * 2013-05-30 2013-07-29 현대중공업 주식회사 A treatment system of liquefied gas

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