KR20150062791A - Treatment system of liquefied gas - Google Patents

Treatment system of liquefied gas Download PDF

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Publication number
KR20150062791A
KR20150062791A KR1020130147796A KR20130147796A KR20150062791A KR 20150062791 A KR20150062791 A KR 20150062791A KR 1020130147796 A KR1020130147796 A KR 1020130147796A KR 20130147796 A KR20130147796 A KR 20130147796A KR 20150062791 A KR20150062791 A KR 20150062791A
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KR
South Korea
Prior art keywords
gas
evaporation
liquefied
evaporative
storage tank
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KR1020130147796A
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Korean (ko)
Inventor
백은성
김주태
김발영
김해천
한주석
Original Assignee
현대중공업 주식회사
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Priority to KR1020130147796A priority Critical patent/KR20150062791A/en
Publication of KR20150062791A publication Critical patent/KR20150062791A/en

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

Abstract

A liquefied gas treatment system according to an embodiment of the present invention comprises: an evaporated gas supply line connected to a liquefied gas storage tank; an evaporated gas compressor disposed on the evaporated gas supply line to pressurize evaporated gas generated in the liquefied gas storage tank; an evaporated gas heat exchanger disposed upstream from the evaporated gas compressor on the evaporated gas supply line to exchange heat between the evaporated gas pressurized by the evaporated gas compressor and then retrieved along the evaporated gas supply line branching downstream of the evaporated gas compressor and the evaporated gas supplied from the liquefied gas storage tank; and a bypass line branching between the liquefied gas storage tank on the evaporated gas supply line and the evaporated gas heat exchanger to bypass downstream of the evaporated gas heat exchanger to join the evaporated gas supply line to supply the evaporated gas to the evaporated gas compressor. The liquefied gas treatment system according to the present invention supplies the evaporated gas generated in the liquefied gas storage tank to the evaporated gas compressor via the bypass line without preheating if the amount of the evaporated gas generated in the liquefied gas storage tank does not exceed an amount requested by a consumer. Therefore, since an increase in volume of the evaporated gas by a temperature does not take place, a load on the evaporated gas compressor can be reduced.

Description

[0001] The present invention relates to a treatment system of liquefied gas,

The present invention relates to a liquefied gas processing system.

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

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

Such liquefied gas is stored in a liquefied gas storage tank installed on the ground or stored in a liquefied gas storage tank provided in a ship which is a means of transporting the ocean. The liquefied natural gas is liquefied to a volume of 1/600 The liquefaction of liquefied petroleum gas has the advantage of reducing the volume of propane to 1/260 and the content of butane to 1/230, resulting in high storage efficiency.

However, since the liquefied gas is kept in a liquefied state by increasing the pressure or lowering the temperature, it is important to secure the heat insulating property of the liquefied gas storage tank because the phase change due to external heat penetration is a concern. However, since the liquefied gas storage tank can not achieve perfect heat insulation, some of the liquefied gas stored in the liquefied gas storage tank is phase-changed into vapor gas, which is a gas, by heat transmitted from the outside.

When the internal pressure of the liquefied gas storage tank exceeds the pressure that can be tolerated by the liquefied gas storage tank, the liquefied gas storage tank The tank may be damaged.

Therefore, conventionally, in order to keep the internal pressure of the liquefied gas storage tank at a constant level, a method has been used in which the evaporation gas is discharged to the outside to lower the internal pressure of the liquefied gas storage tank, if necessary. Or the evaporation gas was discharged to the outside of the liquefied gas storage tank, and then liquefied by using a separate liquefaction device and then recovered again into the liquefied gas storage tank.

However, when the evaporation gas is merely discharged to the outside, a problem of contamination of the external environment may occur, and in the case of using the re-liquefaction device, there arises a problem such as a cost and manpower required for installing and operating the liquefaction device. Therefore, it is required to develop an effective treatment method of the evaporation gas generated by external heat penetration.

Such prior art is disclosed in Korean Registered Patent Publication No. 10-1289212 (Jul. 17, 2013).

The object of the present invention is to improve the prior art. The object of the present invention is to provide an evaporative gas compressor which is capable of increasing the load of the evaporative gas compressor as the evaporative gas generated in the liquefied gas storage tank is preheated by the heat exchange by the evaporative gas supplied from the evaporative gas compressor And it is an object of the present invention to provide a liquefied gas processing system capable of bypassing an evaporating gas heat exchanger in order to prevent an increase in the load of the evaporating gas compressor and protect the evaporating gas heat exchanger when the liquefied flow is not used.

A liquefied gas processing system according to an embodiment of the present invention includes an evaporation gas supply line connected to a liquefied gas storage tank; An evaporative gas compressor provided on the evaporative gas supply line for pressurizing the evaporative gas generated in the liquefied gas storage tank; An evaporative gas provided upstream of the evaporative gas compressor on the evaporative gas supply line and recovered along the evaporative gas supply line which is pressurized in the evaporative gas compressor and branches downstream of the evaporative gas compressor; An evaporative gas heat exchanger for exchanging heat with supplied evaporative gas; And an evaporative gas heat exchanger that is branched from the liquefied gas storage tank on the evaporative gas supply line and the evaporative gas heat exchanger and bypasses downstream of the evaporative gas heat exchanger to join the evaporative gas supply line and supply the evaporative gas to the evaporative gas compressor And a bypass line for causing the second transistor to emit light.

The present invention further includes an evaporative gas decompressor provided downstream of the evaporative gas heat exchanger on the basis of the flow of the evaporative gas recovered along the evaporative gas supply line to decompress the compressed evaporative gas in the evaporative gas compressor .

Further, the present invention is characterized by further comprising a gas-liquid separator for separating the flash gas from the decompressed gas by the evaporation gas decompressor.

And a gas recovery line connected from the gas-liquid separator to an upstream of the evaporation gas heat exchanger to supply the flash gas to the evaporation gas heat exchanger, wherein the evaporation gas heat exchanger includes evaporation- And the gas is cooled by the evaporation gas supplied from the liquefied gas storage tank or the flash gas supplied through the gas recovery line.

In the liquefied gas processing system according to the present invention, when the amount of the evaporated gas generated in the liquefied gas storage tank is not more than that required by the customer, the evaporated gas generated in the liquefied gas storage tank is preheated And then supplied to the evaporative gas compressor, the volume of the evaporative gas due to the temperature is not increased, so that the load of the evaporative gas compressor can be reduced.

In addition, the present invention can prevent evaporation gas generated from the liquefied gas storage tank from leaking through the bypass line and prevent evaporation gas compressor from increasing load and protecting the evaporation gas heat exchanger.

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

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

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

FIG. 1 is a conceptual view of a liquefied gas processing system according to an embodiment of the present invention, and FIG. 2 is a view showing a lubricant separator of a liquefied gas processing system according to an embodiment of the present invention.

1, a liquefied gas processing system 1 according to an embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporative gas compressor 50, an evaporative gas heat exchanger (not shown) 60, an evaporation gas decompressor 80, and a gas-liquid separator 90.

Hereinafter, the liquefied gas may be used to encompass all gaseous fuels generally stored in a liquid state, such as LNG or LPG, ethylene, ammonia, etc. In the case where the gas is not in a liquid state by heating or pressurization, . This also applies to the evaporative gas. In addition, LNG can be used to mean not only NG (Natural Gas) in liquid state but also NG in supercritical state for convenience, and evaporation gas can be used to include not only gaseous evaporation gas but also liquefied evaporation gas have.

The liquefied gas storage tank (10) stores liquefied gas to be supplied to the customer (20). The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, wherein the liquefied gas storage tank 10 may have the form of a pressure tank.

The liquefied gas storage tank 10 may be designed to withstand a pressure of 1 bar to 10 bar (for example 6 bar) consisting of a dual structure tank (not shown) and a heat insulating part (not shown).

Here, a forcing vaporizer (not shown) may be provided between the liquefied gas storage tank 10 and the evaporative gas compressor 50. The forced vaporizer operates when the flow rate of the evaporative gas is insufficient, The flow rate of the evaporation gas supplied to the evaporator can be increased.

In addition, a mixer 70 may be provided between the forced vaporizer and the evaporative gas compressor 50, and the mixer 70 is provided upstream of the evaporative gas heat exchanger 60 on the evaporative gas supply line 16, The flash gas to be supplied from the storage tank 10 can be introduced and the flash gas recovered from the gas-liquid separator 90 can be introduced. The mixer (70) may be in the form of a pressure tank, which is space for storing the evaporating gas and the flash gas.

The customer 20 is driven through the evaporative gas supplied from the liquefied gas storage tank 10 to generate power. At this time, the customer 20 is a high-pressure engine, which may be a gas fuel engine (for example, MEGI).

For example, the customer 20 may be an engine for driving the propeller, but may be an engine for generating power or an engine for generating other power. In other words, the present embodiment does not particularly limit the kind of the consumer 20. However, the customer 20 may be an internal combustion engine that generates a driving force by the combustion of the evaporative gas and the flash gas.

The consumer 20 is supplied with the evaporated gas pressurized by the evaporative gas compressor 50 to obtain the driving force. The state of the evaporative gas supplied to the consumer 20 may vary depending on the state required by the consumer 20.

An evaporation gas supply line 16 for transferring evaporation gas from the liquefied gas storage tank 10 to the customer 20 is installed and the evaporation gas heat exchanger 60 and the evaporation gas compressor 50 ), A customer 20, and the like.

The evaporation gas supply line 16 in this embodiment means to include a refill lining line 16A and a fuel supply line 16B which will be described later and the fuel supply line 16B is a line in the evaporative gas compressor 50, And supplies the pressurized gas to the customer 20. At this time, a fuel supply valve (not shown) is provided in the evaporation gas supply line 16 so that the supply amount of the evaporation gas can be adjusted according to the adjustment of the opening degree of the fuel supply valve.

The evaporative gas compressor (50) pressurizes the evaporative gas generated in the liquefied gas storage tank (10). The evaporation gas compressor 50 can pressurize the evaporation gas generated and discharged from the liquefied gas storage tank 10 and supply the evaporation gas to the evaporation gas heat exchanger 60 or the consumer 20. The plurality of evaporation gas compressors (50) can pressurize the evaporation gas at multiple stages. For example, five evaporation gas compressors 50 may be provided so that the evaporation gas is pressurized in five stages.

The re-liquefaction line 16A as the evaporation gas supply line 16 may be branched between the evaporation gas compressor 50 and the customer 20 and connected to the evaporation gas heat exchanger 60. [ The evaporation gas supply line 16 constitutes the fuel supply line 16B connected to the customer 20 from the evaporative gas compressor 50 or is connected to the refueling line 16A connected to the evaporation gas heat exchanger 60, . At this time, a valve (not shown) is provided on the evaporation gas supply line 16 at the branch point to the evaporation gas heat exchanger 60 so that the flow rate of the evaporation gas can be controlled. In this embodiment, the redistribution line 16A is shown to be branched downstream of the third evaporative gas compressor 50 in the flow of evaporative gas among the five evaporative gas compressors 50, (Not shown).

An evaporative gas cooler (not shown) is provided downstream of each evaporative gas compressor 50 between the plurality of evaporative gas compressors 50 to control the temperature of the evaporated gas, which is pressurized by the evaporative gas compressor 50, Can be lowered again. By increasing the pressure of the evaporating gas to the evaporating gas compressor (50), the evaporating gas can be easily liquefied.

The evaporation gas heat exchanger 60 is provided between the liquefied gas storage tank 10 and the evaporation gas compressor 50 on the evaporation gas supply line 16 and is provided between the evaporation gas pressurized in the evaporation gas compressor 50 and the liquefied gas storage The evaporation gas supplied from the tank 10 can be heat-exchanged. The evaporated gas heat-exchanged in the evaporative gas heat exchanger (60) may be supplied to the evaporative gas decompressor (80) or the evaporative gas compressor (50).

That is, the evaporated gas recovered in the evaporation gas decompressor 80 and the newly supplied evaporated gas in the liquefied gas storage tank 10 after being multi-stage pressurized in the evaporative gas compressor 50 are heat-exchanged in the evaporative gas heat exchanger 60 do.

In this embodiment, the evaporation gas is supplied to the evaporation gas decompressor 80 and the gas-liquid separator 90 via the re-liquefaction line 16A after being pressurized by the evaporation gas compressor 50. [ Here, in order to improve the liquefaction efficiency of the evaporated gas, the evaporated gas pressurized in the evaporated gas compressor 50 is heat-exchanged in the evaporated gas heat exchanger 60.

On the other hand, in the case where the amount of evaporated gas generated in the liquefied gas storage tank 10 is not more than the amount required by the consumer 20, the evaporation gas generated in the liquefied gas storage tank 10 is evaporated Gas refrigerant is pressurized by the evaporative gas compressor 50 via the bypass line 16C bypassing the gas heat exchanger 60 and then supplied to the consumer 20 through the fuel supply line 16B.

The bypass line 16C is branched between the liquefied gas storage tank 10 and the evaporation gas heat exchanger 60 on the evaporation gas supply line 16 and is connected to the evaporation gas supply line 16 to bypass the evaporation gas heat exchanger 60 (16) and supplies the evaporation gas to the evaporation gas compressor (50). Here, a valve 15 is provided on the evaporation gas supply line 16 at the point where the bypass line 16C branches. For example, the valve 15 may be a three-way valve, The amount can be adjusted.

By omitting the preheating of the evaporation gas by bypassing the evaporation gas heat exchanger 60, the volume increase of the evaporation gas can be reduced and the load of the evaporation gas compressor 50 can be reduced. The evaporation gas generated in the liquefied gas storage tank 10 when the liquefied gas is not used can prevent the increase in the load of the evaporative gas compressor 50 and the evaporative gas heat exchanger 60 via the bypass line 16C have. Here, the re-liquefied flow unused is that the evaporated gas discharged from the evaporative gas compressor 50 is passed through the reflux line 16A, the evaporation gas heat exchanger 60, the gas-liquid separator 90 and the gas recovery line 17A The evaporation gas discharged from the evaporative gas compressor 50 may be supplied only to the customer 20 and the re-injection may be omitted.

The mixer (70) A flash gas which is provided upstream of the evaporation gas heat exchanger 60 on the evaporation gas supply line 16 and into which the evaporation gas supplied from the liquefied gas storage tank 10 flows and which is recovered in the gas-liquid separator 90 can be introduced . The mixer (70) may be in the form of a pressure tank, which is space for storing the evaporating gas and the flash gas. Here, the evaporated gas and the flash gas mixed in the mixer 70 are supplied to the evaporative gas heat exchanger 50.

The evaporation gas decompressor 80 pressurizes the evaporated gas heat-exchanged in the evaporation gas heat exchanger 60 after being pressurized by the evaporation gas compressor 50. For example, the evaporation gas decompressor 80 can reduce the pressure of the evaporation gas to 1 bar to 10 bar, the evaporation gas can be liquefied and reduced to 1 bar when transferred to the liquefied gas storage tank 10, The cooling effect can be achieved. For example, the evaporative gas decompressor 80 may reduce the pressure of the evaporated gas pressurized to 300 bar by the evaporative gas compressor 50 to 1 bar. The evaporation gas decompressor 80 may be a line Thompson valve.

The gas-liquid separator 90 separates the gas from the decompressed gas in the gas-gas decompressor 80. In the gas-liquid separator 90, the evaporated gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas can be recovered as flash gas upstream of the evaporative gas compressor 50. Here, the evaporation gas decompressed in the evaporation gas decompressor 80 may be easily liquefied by the lowered temperature, may be recovered to the liquefied gas storage tank 10, and the flash gas generated in the gas-liquid separator 90 And the flash gas can be pressurized through the evaporative gas compressor 50 and then supplied to the consumer 20.

Liquid separator 90 separates the vaporized gas into a liquid and a gas and the liquefied vaporized gas and the flash gas are respectively passed through the liquid recovery line 18 and the gas recovery line 17 to the liquefied gas storage tank 10, (70). ≪ / RTI > The liquid recovery line 18 is connected from the gas-liquid separator 90 to the liquefied gas storage tank 10 to recover the vaporized liquid state to the liquefied gas storage tank 10 and the gas recovery line 17 is connected to the gas- 90 to the mixer 70 upstream of the evaporative gas compressor 50 to recover the flash gas upstream of the evaporative gas compressor 50 to prevent the flash gas from being wasted and wasted.

As described above, in the present embodiment, when the amount of evaporative gas generated in the liquefied gas storage tank 10 is not more than the amount required by the customer 20 and no surplus evaporative gas is generated, the liquefied gas storage tank 10 ) Is supplied to the evaporative gas compressor (50) after the preheating is omitted via the bypass line (16C), the volume of the evaporative gas due to the temperature is not increased, and the load of the evaporative gas compressor (50) Can be saved.

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

The liquefied gas processing system 2 will be described with reference to Fig. The present embodiment is configured such that the flow of the flash gas is different from that of the gas recovery line 17A. The same reference numerals are used to designate the same or corresponding components to those of the above-described embodiment, and redundant description thereof will be omitted.

In this embodiment, the flash gas separated by the gas-liquid separator 90 can be used for heat exchange via the evaporative gas heat exchanger 60A.

The evaporation gas heat exchanger 60A of the present embodiment is provided in the refilling line 16A and is provided with evaporation gas pressurized in the evaporation gas compressor 50 and evaporation gas supplied from the liquefied gas storage tank 10 and gas- The flash gas can be heat-exchanged.

That is, the evaporation gas heat exchanger 60A is provided with evaporation gas recovered along the re-liquefaction line 16A which is pressurized by the evaporation gas compressor 50 and branched at the upstream side of the consumer 20 and evaporation gas recovered from the liquefied gas storage tank 10 Exchanges the supplied evaporation gas. The evaporation gas heat exchanger 60 exchanges heat between the evaporated gas compressed in the evaporative gas compressor 50 and recovered along the evaporated gas supply line 16 and the flash gas supplied through the gas recovery line 17A.

At this time, the evaporation gas heat exchanger 60A cools the evaporative gas recovered along the re-liquefaction line 16A with the evaporation gas supplied from the liquefied gas storage tank 10, or the flash supplied through the gas recovery line 17A It can be cooled with gas. In this case, the evaporated gas recovered along the re-liquefaction line 16A is primarily cooled by the evaporated gas discharged from the liquefied gas storage tank 10, and can be cooled secondarily by the flash gas.

The evaporation gas heat exchanger 60A supplies the evaporation gas supplied from the liquefied gas storage tank 10 to the evaporation gas compressor 50 and supplies the second evaporation gas cooled by the flash gas to the evaporation gas decompressor (80). In this case, since the evaporation gas supplied to the evaporation gas decompressor 80 is cooled not only by the evaporation gas but also by the flash gas, the efficiency of liquefaction due to the reduced pressure can be greatly increased.

The flash gas passing through the evaporative gas heat exchanger 60 may be supplied to a gas combustion unit 100 for burning fuel, a boiler (not shown), or a separate heterogeneous fuel engine (DFDE) (not shown). At this time, the gas recovery line 17A can be extended from the evaporation gas heat exchanger 60A to the mixer 70, and the valve 17B is provided on the gas recovery line 17A, The amount of the flash gas to be supplied to the flash unit 110 can be adjusted.

The evaporation gas decompressed by the evaporation gas decompressor 80 of this embodiment is cooled by the evaporation gas supplied from the liquefied gas storage tank 10 and cooled by the flash gas supplied from the gas-liquid separator 90 Therefore, sufficient re-liquidation can be achieved. That is, this embodiment can utilize the cold heat of the flash gas, so that the re-liquefaction efficiency higher than that using the heat exchange between the evaporated gases can be obtained.

In addition, in the present embodiment, the evaporated gas heated to a temperature of around 45 degrees is recovered by the evaporated gas heat exchanger 60, and the evaporated gas of about -100 degrees and -150 degrees supplied from the liquefied gas storage tank 10, Exchanged with the flash gas, cooled to a temperature of about -95 ° C or lower, and supplied to the evaporation gas decompressor 80. At this time, in the evaporation gas decompressor 80, the evaporation gas is cooled by the reduced pressure and can have a pressure of about 3 bar and a temperature of about -150.2 degrees.

At this time, the evaporation gas has a temperature lower than the boiling point at 3 bar, so that at least a part can be liquefied and the remainder can be present as gaseous flash gas. In this case, the flash gas also has a state of about -150 degrees, and the flash gas of -150 degrees is supplied to the evaporation gas heat exchanger 60 in the gas-liquid separator 90 and can be used to cool the evaporation gas.

As described above, in this embodiment, the evaporation gas supplied to the gas-liquid separator 90 is sufficiently cooled by the evaporation gas and the flash gas in the evaporation gas heat exchanger 60 and then decompressed to 3 bar in the evaporation gas decompressor 80, So that the liquefaction efficiency of the evaporation gas can be improved.

In this embodiment, liquefied evaporated gas can be recovered in the liquefied gas storage tank 10, and the flash gas generated in the gas-liquid separator 90 can be recovered in the evaporative gas heat exchanger 60 to heat-exchange the evaporated gas .

Liquid separator 90 separates the vaporized gas into a liquid and a gas and the liquefied vapor gas and the flash gas respectively flow through the liquid recovery line 18 and the gas recovery line 17 to the liquefied gas storage tank 10, Gas heat exchanger (60).

The liquid recovery line 18 is connected from the gas-liquid separator 90 to the liquefied gas storage tank 10 to recover the vaporized liquid state to the liquefied gas storage tank 10 and the gas recovery line 17 is connected to the gas- 90 to the evaporation gas heat exchanger 60 to recover the flash gas to the evaporation gas heat exchanger 60 to heat exchange the evaporation gas.

In the present embodiment, when the amount of evaporated gas generated in the liquefied gas storage tank 10 is smaller than the amount required in the consumer 20, the evaporated gas generated in the liquefied gas storage tank 10 flows into the bypass line 16C And then the evaporation gas compressor 50 is supplied with the preheating gas, the volume of the evaporation gas due to the temperature does not increase, and the load of the evaporation gas compressor 50 can be reduced.

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

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

1,2: liquefied gas processing system 10: liquefied gas storage tank
15, 17B: valve 16: evaporation gas supply line
16A: Re-liquefaction line 16B: Fuel supply line
16C: bypass line 17,17A: gas recovery line
18: liquid recovery line 20: customer
50: Evaporative gas compressor 60, 60A: Evaporative gas heat exchanger
70: Mixer 80: Evaporative gas decompressor
90: gas-liquid separator 100: gas combustion unit

Claims (4)

An evaporation gas supply line connected to the liquefied gas storage tank;
An evaporative gas compressor provided on the evaporative gas supply line for pressurizing the evaporative gas generated in the liquefied gas storage tank;
An evaporative gas provided upstream of the evaporative gas compressor on the evaporative gas supply line and recovered along the evaporative gas supply line which is pressurized in the evaporative gas compressor and branches downstream of the evaporative gas compressor; An evaporative gas heat exchanger for exchanging heat with supplied evaporative gas; And
The evaporated gas heat exchanger is branched from the liquefied gas storage tank on the evaporation gas supply line and the evaporation gas heat exchanger and bypasses downstream of the evaporation gas heat exchanger to join the evaporation gas supply line to supply the evaporation gas to the evaporation gas compressor And a bypass line. The method according to claim 1,
Further comprising an evaporative gas decompressor provided downstream of the evaporative gas heat exchanger on the basis of a flow of the evaporative gas recovered along the evaporative gas supply line to decompress the compressed evaporative gas in the evaporative gas compressor, Gas treatment system. 3. The method of claim 2,
Further comprising a gas-liquid separator for separating the flash gas from the evaporated gas decompressed by the evaporative gas decompressor. The method of claim 3,
And a gas recovery line connected from the gas-liquid separator to an upstream side of the evaporation gas heat exchanger to supply the flash gas to the evaporation gas heat exchanger,
Wherein the evaporation gas heat exchanger is configured to cool the evaporation gas recovered along the evaporation gas supply line to an evaporation gas supplied from the liquefied gas storage tank or a flash gas supplied through the gas recovery line system.
KR1020130147796A 2013-11-29 2013-11-29 Treatment system of liquefied gas KR20150062791A (en)

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KR20170001251A (en) * 2015-06-26 2017-01-04 삼성중공업 주식회사 Fuel gas supply system
KR20170001250A (en) * 2015-06-26 2017-01-04 삼성중공업 주식회사 Fuel gas supply system
KR20170011685A (en) * 2015-07-24 2017-02-02 삼성중공업 주식회사 Fuel gas supplying system in ships
JP2019509937A (en) * 2016-03-31 2019-04-11 デウ シップビルディング アンド マリン エンジニアリング カンパニー リミテッド Evaporative gas reliquefaction apparatus and evaporative gas reliquefaction method
WO2024018873A1 (en) * 2022-07-20 2024-01-25 三菱造船株式会社 Floating body

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KR20170001251A (en) * 2015-06-26 2017-01-04 삼성중공업 주식회사 Fuel gas supply system
KR20170001250A (en) * 2015-06-26 2017-01-04 삼성중공업 주식회사 Fuel gas supply system
KR20170011685A (en) * 2015-07-24 2017-02-02 삼성중공업 주식회사 Fuel gas supplying system in ships
JP2019509937A (en) * 2016-03-31 2019-04-11 デウ シップビルディング アンド マリン エンジニアリング カンパニー リミテッド Evaporative gas reliquefaction apparatus and evaporative gas reliquefaction method
US11760462B2 (en) 2016-03-31 2023-09-19 Daewoo Shipbuilding & Marine Engineering Co., Ltd. Boil-off gas re-liquefying device and method for ship
WO2024018873A1 (en) * 2022-07-20 2024-01-25 三菱造船株式会社 Floating body

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