KR20170049663A - A ReGasification System Of Liquefied Gas - Google Patents

Abstract

According to the present invention, a system for re-gasifying liquefied gas includes: a gasifying portion configured to gasify liquefied gas stored in a liquefied gas storage tank; a heat exchanger configured to heat-exchange liquefied gas, discharged from the gasifying portion and at least partially returning, with liquefied gas supplied from the liquefied gas storage tank, and to be provided in an upper area of the gasifying portion; and a liquefier configured to decompress or expand the liquefied gas discharged from the gasifying portion and heat-exchanged by the heat exchanger, thereby gasifying the liquefied gas. As such, the present invention enables a re-gasification process to quickly proceed and enables a reliable re-gasification operation.

Description

A ReGasification System of Liquefied Gas}

The present invention relates to a liquefied gas regeneration system.

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 less under 1 atm of the main component. The volume of liquefied methane is about 1/600 of the volume of methane in a gaseous state in a standard state, Is 0.42, which is about one half of the specific gravity of crude oil.

LNG is liquefied with ease of transportation and used after vaporizing at the place of use after transportation. However, due to the risk of natural disasters and terrorism, it is feared to install LNG vaporization equipment onshore.

As a result, in place of the conventional liquefied natural gas regeneration system installed on the land, a system for supplying natural gas that is vaporized on the land by installing a regeneration device on an LNG carrier carrying the liquefied natural gas Is in the spotlight.

In the LNG regasifier system, the LNG stored in the liquefied gas storage tank is pressurized by the booster pump and sent to the LNG vaporizer, which is vaporized by the LNG vaporizer and sent to the onshore consumer. Here, a large amount of energy is required in the process of heat exchange in which the temperature of the LNG is increased on the LNG vaporizer. Therefore, in order to solve the problem that the energy used in this process is wasted due to inefficient exchange, various heat exchange techniques for efficient regeneration have been studied.

SUMMARY OF THE INVENTION The present invention has been made to improve the conventional art, and it is an object of the present invention to provide a liquefied gas regeneration system that enables rapid regeneration process and reliable regeneration drive.

A liquefied gas regeneration system according to the present invention includes: a vaporizer for vaporizing a liquefied gas stored in a liquefied gas storage tank; A heat exchanger for exchanging heat between the liquefied gas discharged from the vaporizing unit and returned at least partially to the liquefied gas supplied from the liquefied gas storage tank; And a liquefier for liquefying or expanding the liquefied gas discharged from the vaporizing unit and heat-exchanged in the heat exchanger.

Specifically, a first pump for supplying liquefied gas stored in the liquefied gas storage tank; A temporary storage tank for temporarily storing the liquefied gas supplied from the first pump; And a second pump for pressurizing the liquefied gas supplied from the temporary storage tank, wherein the vaporizing unit is configured to vaporize the liquefied gas supplied by the first pump by first vaporizing the liquefied gas by the first vaporized fuel A first vaporizer; And a second vaporizer for transferring a heat source to the first vaporized fruit or directly vaporizing the liquefied gas directly.

Specifically, the liquefied gas may further include a gas combustion device for burning the evaporated gas evaporated by thermal penetration.

Specifically, the gas liquefied in the liquefier may be supplied to the temporary storage tank.

Specifically, the temporary storage tank may be configured such that liquefied gas supplied from the liquefier and liquefied gas supplied from the liquefied gas storage tank are mixed and separated into a liquid phase and a vapor phase, the liquid phase is supplied to the second pump, The gas phase can be supplied to the gas combustion device.

Specifically, the heat exchanger is a first heat exchanger, and includes a second heat exchanger for exchanging heat between evaporated gas generated in the liquefied gas storage tank and liquefied gas in the liquefier; And a gas-liquid separator for separating the evaporated gas heat-exchanged in the second heat exchanger and the liquefied gas into a liquid phase and a vapor phase.

Specifically, the evaporated gas supplied to the second heat exchanger from the liquefied gas storage tank may be combined with the gas separated from the temporary storage tank or the gas separated from the gas-liquid separator and supplied to the second heat exchanger.

Specifically, the gas-liquid separator can merge the separated gas with the vaporized gas supplied from the liquefied gas storage tank to the second heat exchanger, and return the separated liquid to the liquefied gas storage tank.

Specifically, when the demanded consumer consuming the liquefied gas vaporized by the vaporizing unit malfunctions or the amount accommodated by the demanded consumer is equal to or larger than the predetermined capacity, at least a part or the whole of the liquefied gas vaporized by the vaporizing unit as the heat exchanger Can be supplied.

Specifically, when the vaporizing unit is malfunctioning, the heat exchanger may be supplied with the entire amount of the fluid discharged from the vaporizing unit.

The liquefied gas regeneration system according to the present invention has a purging gas and a drain vessel to effectively prevent icing of the intermediate fruit in the re-gasification heat exchanger using seawater and to improve the reliability of the regeneration process.

In the liquefied gas regeneration system according to the present invention, the indirect vaporization method using steam and the direct vaporization method of steam are applied, and the direct vaporized steam is supplied to the preliminary vaporizer at the previous stage to diversify the vaporization berries Thus, the vaporization operation cost is optimized, the driving reliability is improved through various vaporization routes, and the stabilization of the re-ignition drive due to the freezing of the vaporized vapor is prevented, thereby improving the driving stability.

Further, the liquefied gas regeneration system according to the present invention has an ejector in place of a compressor for the processing of surplus BOG, thereby reducing construction cost, power consumption, and reliability .

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

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

Hereinafter, the liquefied gas may be 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 encompass both NG (natural gas), which is a liquid state, and NG, which is a supercritical state for the sake of convenience. The LNG may be used to mean not only a gas state evaporation gas but also a liquefied evaporation gas .

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 regeneration system according to a first embodiment of the present invention.

1, the liquefied gas regeneration system 1 according to the first embodiment of the present invention includes a liquefied gas storage tank 10, a first pump 21, a buffer tank 22, a second A gas purifying device 51, and a gas detecting device 60. The pump 23, the vaporization first heat exchanger 241a, the vaporization second heat exchanger 251a, the customer 30, the gas combustion unit 40, ). Here, the ship equipped with the liquefied gas regeneration system 1 is equipped with a liquefied gas regeneration system (not shown) in the liquefied gas carrier line (not shown) so as to regenerate the liquefied gas at sea and supply the liquefied gas to the land terminal (LNG RV) or a floating liquefied gas storage and regasification facility (FSRU) equipped with a liquefied natural gas (LNG) 1.

Hereinafter, a liquefied gas regeneration system 1 according to a first embodiment of the present invention will be described with reference to Fig.

The embodiment of the present invention may further include the first to sixth lines L1 to L6, the glycol water line GL, the first to third lines SL1 to SL3 and the heating line HL . Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The first line L1 connects the liquefied gas storage tank 10 and the demander 30 and includes a first pump 21, a buffer tank 22, a second pump 23, a vaporization first heat exchanger 241a and a vaporization second heat exchanger 251a and can supply the liquefied gas of the liquefied gas storage tank 10 to the consumer 30 through the first pump 21 and the second pump 23 have.

The second line L2 connects the liquefied gas storage tank 10 and the gas combustion device 40 and can supply the evaporated gas of the liquefied gas storage tank 10 to the gas combustion device 40. [ At this time, the second line L2 is connected to the gas combustion device 40, but any gas can be used as long as it can consume the evaporation gas and is not limited to the gas combustion device 40.

The third line L3 may be branched between the vaporization first heat exchanger 241a and the vaporization second heat exchanger 251a on the first line L1 and directly connected to the gas combustion device 40, May be branched between the vaporization first heat exchanger 241a and the vaporization second heat exchanger 251a on the line L1 and connected on the fourth line L4.

The fourth line L4 connects the buffer tank 22 and the gas combustion device 40 or connects the buffer tank 22 and the third line L3 to connect the gas generated in the buffer tank 22 And can be supplied to the gas combustion apparatus 40.

The fifth line L5 is connected between the purge device 51 and the vaporized first heat exchanger 241a and the first vaporized second control valve 245 on the glycol water line GL to provide a purge device 51 ) Can be supplied onto the glycol water line GL.

The sixth line L6 may be branched on the glycol water line GL between the vaporizing first heat exchanger 241a and the first vaporizing first control valve 244 and connected to the temporary storage tank 54 , The purging gas of the purging device 51 purges the first vaporized beryllium (glycol water) frozen in the vaporizing first heat exchanger 241a to receive and temporarily store the fluids discharged together.

The glycol water line GL is connected to the vaporized first heat exchanger 241a, the first vaporized liquid heat exchanger 242a, the first vaporized liquid feed pump 243a, the first vaporized liquid first regulating valve 244a ), A first vaporization second control valve 245, and the first water vaporization glycol water flows to circulate the components.

The first seawater first line SL1 is provided with a second vaporized fruit feed pump 261 and a first vaporized fruit heat exchanger 242a for supplying seawater to the first vaporized fruit heat exchanger 261 through the second vaporized fruit feed pump 261, So that it can be supplied to the unit 242a.

The second seawater line SL2 is branched between the second vaporization feed pump 261 and the first vaporization heat exchanger 242a on the first line SL1 of seawater and is connected to the first vaporization heat exchanger 242a And is connected to the first line SL1 of the seawater again by bypassing, and may include the vaporization second heat exchanger 251a. Here, the second seawater line SL2 can supply at least a part of the seawater flowing on the first seawater line SL1 to the vaporization second heat exchanger 251a.

The third seawater line SL3 is branched on the seawater second line SL2 to the inlet end of the vaporization second heat exchanger 251a and then flows into the vaporization second heat exchanger 251a on the second seawater line SL2, And a second vaporization heat exchanger 252a may be provided. The third seawater line SL3 supplies at least a part of the seawater flowing on the seawater second line SL2 to the second vaporization heat exchanger 252a to be heated, As shown in FIG.

The heating line HL may include a second vaporization heat exchanger 252a and a heater 80 as a closed loop line so that the heating fruit flows to heat the seawater as the second vaporization fruit to circulate the configurations can do.

The liquefied gas storage tank (10) stores liquefied gas to be supplied to the customer (30). The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, at which time the liquefied gas storage tank 10 may have the form of a pressure tank.

Here, the liquefied gas storage tank 10 is not limited to various types.

The first pump 21 is disposed on the first line L1 and is installed inside or outside the liquefied gas storage tank 10 to store the liquefied gas stored in the liquefied gas storage tank 10 in the buffer tank 22, . In this case, the first pump 21 may be a latent pump when it is provided inside the liquefied gas storage tank 10, or may be a centrifugal pump when it is installed outside the liquefied gas storage tank 10.

The buffer tank 22 is provided on the first line L1 and is provided between the liquefied gas storage tank 10 and the second pump 23 to supply the liquefied gas to the second pump 23 The liquefied gas supplied from the first pump 21 can be temporarily stored. Specifically, the buffer tank 22 can receive the liquefied gas stored in the liquefied gas storage tank 10 from the first pump 21, temporarily store the liquefied gas, and separate the liquid phase and the vapor phase, (23), and the gas phase can be supplied to the gas combustion device (40) to be described later.

That is, the buffer tank 22 temporarily stores the liquefied gas to separate the liquid phase and the vapor phase, and supplies the complete liquid phase to the second pump 23 so that the second pump 23 satisfies the effective suction head, This makes it possible to prevent cavitation in the second pump 23.

The second pump 23 may be provided between the buffer tank 22 and the vaporization first heat exchanger 241a on the first line L1 and may supply the liquefied gas supplied from the first pump 21 to the high pressure And supplied to the vaporization first heat exchanger 241a.

The second pump 23 is constituted by a boosting pump and can pressurize the liquefied gas in accordance with the pressure demanded by the customer 30 and can be constituted by a centrifugal pump.

The vaporization first heat exchanger 241a may be provided between the second pump 23 and the vaporization second heat exchanger 251a on the first line L1 and may be provided between the second pump 23 and the vaporization second heat exchanger 251a, It is possible to supply the gas to the first gasification by supplying the heat source.

The vaporization first heat exchanger 241a may use a heating medium having a temperature of a freezing point lower than that of water as the first vaporization heat and may include, for example, propane, ethane, ammonia, glycol It may be a glycol water, most preferably a glycol water free from fire hazards and easy to handle.

In the embodiment of the present invention, in order to vaporize the liquefied gas through the first vaporized fuel to the vaporized first heat exchanger 241a, the first vaporized heat exchanger 242a, the first vaporized liquid feed pump 243a, A first vaporizing first regulating valve 244, a first vaporizing second regulating valve 245 and a glycol water line GL.

The vaporized first heat exchanger 241a is connected to the glycol water line GL and the first line L1 so that the liquefied gas is discharged from the first line L1 and the liquefied gas is discharged from the glycol water line GL, The liquefied gas can be cooled by being supplied with the heat source from the first vaporized liquid and vaporized, and the first vaporized liquid can be cooled by receiving the cold heat from the liquefied gas.

The glycol water line GL includes a first vaporization heat exchanger 242a, a first vaporization feed pump 243a, first vaporization first and second control valves 244 and 245, The first vaporized fuel supplied from the first vaporized heat exchanger 242a through the supply pump 243a is supplied to the vaporized first heat exchanger 241a and then supplied to the first vaporized thermal heat exchanger 242a Can be circulated.

The first vaporization heat exchanger 242a may be provided between the first vaporization feed pump 243a and the first vaporization second control valve 245 on the glycol water line GL, The first vaporized water supply line GL is connected to the first seawater first line SL1 so that the second vaporized fruit is supplied from the second vaporized fruit supply pump 261 through the seawater first line SL1, The first vaporized fruit and the second vaporized fruit can be heat-exchanged with each other by receiving the first vaporized fruit.

Here, the first vaporization heat exchanger 242a is supplied with the second vaporization energy from the second vaporization energy supply pump 261, which will be described later, to be heat-exchanged with the first vaporization energy to receive the heat source, Is heated by the second vaporized fruit, and the second vaporized fruit can be cooled by the first vaporized fruit.

The first vaporization feed pump 243a is provided between the first vaporization feed first control valve 244 and the first vaporization heat exchanger 242a on the glycol water line GL to feed the glycol water line GL, (Glycol water) flowing on the first vaporized water (glycol water) can circulate, or can be a centrifugal pump.

The first vaporization first regulating valve 244 is provided between the vaporization first heat exchanger 241a and the first vaporization feed pump 243a on the glycol water line GL and through the valve opening / Can regulate the circulation or retention of the first vaporized fruit flowing on the glycol water line (GL).

The first vaporization second control valve 245 is provided between the vaporization first heat exchanger 241a and the first vaporization heat exchanger 242a on the glycol water line GL and through the valve opening / Can regulate the circulation or retention of the first vaporized fruit flowing on the glycol water line (GL).

The vaporized second heat exchanger 251a may be provided between the vaporized first heat exchanger 241a and the consumer 30 on the first line L1 and may be provided between the vaporized first heat exchanger 241a and the consumer 30, The heat source can be supplied to the secondary liquefied gas to raise the temperature of the primary gasified liquefied gas to the secondary gasified or primary vaporized liquefied gas.

Here, the secondary vaporization means completely vaporizing the liquefied gas at least partially vaporized during the first vaporization, and the vaporization second heat exchanger 251a may be a medium for transferring the heat source to the first vaporized liquid, Sea Water.

The vaporized second heat exchanger 251a is connected to the seawater second line SL2 and the first line L1 so that liquefied gas is discharged from the first line L1 to the second line The liquefied gas can be cooled by being supplied with the heat source from the second vaporized fuel and vaporized, and the second vaporized liquid can be cooled by receiving the cold heat from the liquefied gas.

Here, the vaporization second heat exchanger 251a is a direct vaporization system in which a direct heat source is supplied and vaporized by the second vaporization heat, and the vaporization first heat exchanger 241a is configured to heat the second vaporization heat source from the first vaporization heat Indirect vaporization can be followed indirectly by vaporization.

In the embodiment of the present invention, the second vaporized heat exchanger 252a, the second vaporized liquid feed pump 261, and the second vaporized liquid feed pump 261 are provided in order to vaporize the liquefied gas through the second vaporized liquid to the vaporized second heat exchanger 251a. A heater 80, and seawater first through third lines SL1 through SL3.

The second vaporization heat exchanger 252a is provided on the third seawater line SL3 and supplies seawater supplied at least partially from the second seawater line SL2 to the heater 80 via the heater 80 and the heater line HL Heat exchange can be performed with the heat source. At this time, the sea water can be heated by the heater 80 to raise the temperature.

The second vaporization feed pump 261 can supply a second vaporized liquid (sea water) that is provided on the first line SL1 of seawater and flows on the first line SL1 of the seawater, have.

The customer 30 can supply and consume the liquefied gas vaporized by the vaporization first heat exchanger 241a and the vaporization second heat exchanger 251a. Here, the customer 30 may be a terrestrial terminal installed on the land, which can vaporize the liquefied gas and supply and use the liquefied gas in the gas phase.

The gas combustion device 40 is a device in which the vaporized gas generated in the liquefied gas storage tank 10 through the second line L2 and the liquefied gas vaporized in the vaporized first heat exchanger 241a through the third line L3 , And the fourth line (L4) to supply the evaporated gas generated in the buffer tank (22) and burn it.

The purging device 51 is configured to be connected to the glycol water line GL by a fifth line L5 and is configured to store a high pressure purging gas (preferably an inert gas, more preferably nitrogen gas) It can have a high-pressure vessel form.

The purging device 51 supplies the high pressure purging gas to the glycol water line GL between the vaporization first heat exchanger 241a and the first vaporization second control valve 245 by the fifth line L5 Thereby purging the first vaporized or freezing fluid in the vaporized first heat exchanger 241a.

An embodiment of the present invention is directed to a purging first regulating device 52 (not shown) for purging the first vaporized fluid or residual fluid that is freezing on the glycol water line GL provided in the vaporization first heat exchanger 241a ), A second purifying device (53), and a temporary storage tank (54).

The purging first regulating device 52 is provided on the fifth line L5 and is capable of regulating the supply amount of the purging gas flowing on the fifth line L5 through the opening and closing control of the valve, The device 53 is provided on the sixth line L6 and can regulate the supply amount of the purging gas flowing on the sixth line L6 through the opening and closing of the valve.

The temporary storage tank 54 is connected to the glycol water line GL by the sixth line L6 and is connected to the glycol water line GL in the vaporization first heat exchanger 241a via the purging gas supplied from the purging device 51. [ It is possible to store the first vaporized berries freezing in the glazing unit GL together with the purging gas, and to constitute a high-pressure vessel for temporarily storing the high-pressure purging gas. In this case, the temporary storage tank 54 temporarily stores and separates the high-pressure purging gas to re-supply the first vaporized fruit to the glycol water line GL or to discharge the high-pressure purging gas and the first vaporized fruit to the outside have.

In the present invention, since the first vaporized liquid flowing into the vaporized first heat exchanger 241a is cooled by being deprived of the heat source from the liquefied gas, a heating medium having a freezing point lower than that of water is used to prevent freezing. However, when the flow of the first vaporized liquid is slowed and the time for exposing to the liquefied gas is prolonged and the cold heat is excessively supplied, or when heat exchange with the liquefied gas is performed in a state where the heat capacity of the first vaporized liquid is small, The freezing of the vaporized first heat exchanger 241a may occur suddenly and the solidification of the vaporized first heat exchanger 241a may weaken the durability of the vaporized first heat exchanger 241a, have.

Therefore, in the embodiment of the present invention, the purge device 51 and the purge first control device 52, the purging second control device 53, and the temporary storage tank 54 are provided to prevent the above- 1 heat exchanger 241a is prevented from freezing and a purging device 51 and a purging first adjusting device 52 to prevent icing and a purging second adjusting device 53 and a temporary storage tank 54 The mechanism will be described below.

In the present invention, when it is judged by the gas detection device 60 to be described later whether or not the vaporized first heat exchanger 241a is freezing (in the embodiment of the present invention, the first vaporized liquid freezing in the vaporized first heat exchanger 241a However, the present invention is not limited to the gas detection device 60, and is not necessarily limited to the gas detection device 60, and it may be determined whether or not the first vaporized liquid in the vaporization first heat exchanger 241a is freeze The driving of the first pump 21 or the second pump 23 is stopped to prevent the supply of the liquefied gas to the customer 30 and the supply of the liquefied natural gas to the first vaporizing liquid feed pump 243a The driving can be stopped and the circulation of the first vaporized fruit on the glycol water line GL can be stopped.

Thereafter, the opening of the first vaporizing first regulating valve 244 and the first vaporizing second regulating valve 245 is closed and the high-pressure purge stored in the purging device 51 through the purging first regulating device 52 The gas can be supplied to the glycol water line (GL). Thereby purging the first vaporized fruit that has frozen on the glycol water line GL in the vaporization first heat exchanger 241a, and the purged first vaporized fruit and the purging gas are purged by the purging second regulator 53 To the temporary storage tank 54 and temporarily stored.

When all of the first vaporized fruits that have been frozen on the glycol water line GL in the vaporized first heat exchanger 241a are purged by the purging device 51, the purging first regulating device 52 and the purging second regulating device The supply of the purging gas is prevented through the device 53 and the opening of the first vaporizing first regulating valve 244 and the first vaporizing second regulating valve 245 is opened and then the first vaporizing fruit feeding pump 243a The first pump 21 or the second pump 23 is driven to return the liquefied gas stored in the liquefied gas storage tank 10 to the regeneration state And can supply it to the customer 30.

Thus, in the embodiment of the present invention, the purging device 51 and the purging first regulating device 52, the purging second regulating device 53, and the temporary storage tank 54 are provided, and the vaporized first heat exchanger 241a The vaporization efficiency of the liquefied gas regeneration system 1 can be improved and the driving reliability of the liquefied gas regeneration system 1 can be improved.

The gas detection device 60 can be provided between the customer 30 and the vaporization second heat exchanger 251a on the first line L1 and can detect the state of the vaporized liquefied gas supplied to the customer 30 It is possible to detect the flow amount of the liquefied gas, the pressurized state of the liquefied gas, the supply of the liquefied gas to the customer 30, and the like.

Here, the type of the gas detecting device 60 is not limited, and may be a pressure measuring sensor, a flow measuring sensor, or a gas detecting sensor.

The gas detection device 60 can detect the amount of the vaporized liquefied gas supplied to the customer 30 and can detect the amount of the vaporized liquefied gas supplied to the customer 30 or reduce the amount of vaporized liquefied gas It is possible to detect that the liquefied gas is supplied. Thus, in the present invention, it can be understood that the first vaporized fruit on the glycol water line (GL) in the vaporization first heat exchanger (241a) is frozen.

As described above, the liquefied gas regeneration system 1 according to the first embodiment of the present invention is provided with the purge device 51 and the temporary storage tank 54 serving as the drain container, so that the first vaporizer 241a using seawater, It is possible to effectively prevent the freezing of the fruit and thereby the rebigging rate of the re-evaporation process is rapidly increased, preventing the waste of the re-burned energy and improving the reliability of the re-burning process.

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

2, the liquefied gas regeneration system 2 according to the second embodiment of the present invention includes a liquefied gas storage tank 10, a first pump 21, a buffer tank 22, A pump 23, a vaporization first heat exchanger 241b, a vaporization second heat exchanger 251b, a first heat exchanger 27a, a liquefier 28, a customer 30, a gas combustion unit (gas combustion unit) 40).

The configuration other than the vaporized first heat exchanger 241b, the vaporized second heat exchanger 251b, the first heat exchanger 27a, the liquefier 28, and the gas combustion device 40 in the second embodiment of the present invention, The same reference numerals are used for the respective constitutions and the like in the first embodiment of the invention, but they are not necessarily referred to the same constructions.

The ship equipped with the liquefied gas regeneration system 2 here is provided with a liquefied gas carrier line (not shown) for re-liquefying the liquefied gas at sea and supplying the liquefied gas to the land terminal, A liquefied gas regasification vessel (LNG RV) or a floating liquefied gas storage and regasification facility (FSRU) with the system 2 installed therein.

Hereinafter, a liquefied gas regeneration system 2 according to a second embodiment of the present invention will be described with reference to Fig.

The vaporized first heat exchanger 241b may be provided between the first heat exchanger 27a and the vaporization second heat exchanger 251b on the first line L1 and may be supplied from the first heat exchanger 27a It is possible to supply the heat source to the liquefied gas to be vaporized.

The vaporization first heat exchanger 241b may use a heating medium having a temperature of a freezing point lower than that of water as the first vaporization heat and may include, for example, propane, ethane, ammonia, It may be a glycol water, most preferably a glycol water free from fire hazards and easy to handle.

In the embodiment of the present invention, in order to vaporize the liquefied gas through the first vaporized fuel to the vaporized first heat exchanger 241b, the first vaporized heat exchanger 242b, the first vaporized liquid feed pump 243b, And may further include a water line GL.

The vaporized first heat exchanger 241b is connected to the glycol water line GL and the first line L1 so that the liquefied gas is discharged from the first line L1 and the liquefied gas is discharged from the glycol water line GL, The liquefied gas can be cooled by being supplied with the heat source from the first vaporized liquid and vaporized, and the first vaporized liquid can be cooled by receiving the cold heat from the liquefied gas.

The first vaporization heat exchanger 242b may be provided between the first vaporization feed pump 243b and the vaporization first heat exchanger 241b on the glycol water line GL, And the steam second line St2 are connected together so that the second vaporized liquid distributed by the second vaporizing liquid distributor 262 from the second vaporizing liquid feed pump (not shown) is supplied to the steam second line St2 And the first vaporized berries may be supplied through the glycol water line (GL) to exchange heat between the first vaporized beryllium and the second vaporized beryllium.

Here, the first vaporization heat exchanger 242b may receive the second vaporization heat from the second vaporization heat distributor 262, which will be described later, and heat-exchange the first vaporization heat with the first vaporization heat, Is heated by the second vaporized fruit, and the second vaporized fruit can be cooled by the first vaporized fruit.

The first vaporization feed pump 243b can circulate the first vaporized fruit (glycol water) which is provided on the glycol water line GL and flows on the glycol water line GL, .

The vaporized second heat exchanger 251b may be provided between the vaporized first heat exchanger 241b and the consumer 30 on the first line L1 and may be provided between the vaporized first heat exchanger 241b and the consumer 30, By supplying a source of heat to the vaporized liquefied gas, the temperature of the initially vaporized liquefied gas can be increased or the temperature of the initially vaporized liquefied gas can be increased.

Here, the additional vaporization means completely vaporizing the at least partially vaporized liquefied gas during the initial vaporization, and the vaporization second heat exchanger 251b may be a medium for transferring the heat source to the first vaporized liquid, Steam).

The vaporized second heat exchanger 251b is connected to the third line St3 and the first line L1 so that the liquefied gas is supplied from the first line L1 to the second vaporized liquid distributor 262, The second vaporized fruits distributed through the third vapor line St3 can be supplied directly through the steam third line St3 and the supplied liquefied gas and the second vaporized liquid can be exchanged with each other and the liquefied gas can be supplied And the second vaporized fruit can be cooled by receiving cold heat from the liquefied gas.

Here, the vaporization second heat exchanger 251b is a direct vaporization system in which the vaporization source directly receives a heat source and is vaporized. The vaporization first heat exchanger 241b is configured to vaporize the second vaporization heat source from the first vaporization source Indirect vaporization can be followed indirectly by vaporization.

In the embodiment of the present invention, in order to further vaporize the liquefied gas through the second vaporized liquid to the vaporized second heat exchanger 251b, the second vaporized liquid that distributes the second vaporized liquid flowing on the steam first line (St1) The vaporization distributor 262 and the steam third line St3.

The second vaporization heat distributor 262 may be configured such that when the vaporized first heat exchanger 241b malfunctions or the first vaporized liquid fails to vaporize the liquefied gas due to freezing or the first vaporized liquid feed pump 243b, The first vaporized heat exchanger 242b reduces the supply amount of the second vaporized heat to a predetermined value and the second vaporized heat is exchanged to the vaporized second heat exchanger 251b by the first vaporized heat exchanger 242b, So that the liquefied gas that is not vaporized by the vaporization first heat exchanger 241b can be completely vaporized.

Of course, in the case where the vaporized second heat exchanger 251b malfunctions, the second vaporized liquid distributor 262 increases the supply amount of the second vaporized liquid to the first vaporized liquid heat exchanger 242b by a predetermined value, The second heat exchanger 251b can reduce the supply amount of the second vaporized heat to a value larger than a preset value so that the vaporized first heat exchanger 241b can completely vaporize the liquefied gas.

That is, the second vaporization / distribution unit 262 controls the supply amount of the second vaporized fuel according to whether the vaporization first heat exchanger 241b and the vaporization second heat exchanger 251b are disabled or not, When the operation of the heat exchangers 241b and 251b is completely disabled, the second vaporized fruits can be completely supplied to the operable heat exchanger and the supply to the non-operable heat exchanger can be stopped.

Thus, in the embodiment of the present invention, even if the vaporized first heat exchanger 241b malfunctions or the first vaporized liquid can not freeze and evaporate the liquefied gas, the liquefied gas regeneration system 2 is driven The liquefied gas can be continuously regenerated without stopping the operation of the regeneration system 2, thereby improving the driving reliability of the regeneration system 2.

The embodiment of the present invention may further include bypass first and second lines BL1 to BL2. Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The bypass first line BL1 branches from the vaporization second heat exchanger 251b on the first line L1 to the customer 30 and is connected to a first heat exchanger 27a to be described later, The flow rate of the liquefied gas that is bypassed to the first heat exchanger 27a can be adjusted through the heat exchanger (not shown). Here, the bypass first line BL1 is branched between the vaporization first heat exchanger 241b and the vaporization second heat exchanger 251b on the first line L1 to supply the liquefied gas to the vaporization second heat exchanger 251b Thereby contributing to improvement in durability of the vaporization second heat exchanger 251b.

The bypass second line BL2 may include a liquefier 28 that connects the first heat exchanger 27a and the buffer tank 22 and may include a first heat exchanger 27a and a liquefier 28, The liquefied liquefied gas can be supplied to the buffer tank 22.

The first heat exchanger 27a may be provided between the second pump 23 and the vaporization first heat exchanger 241b on the first line L1 and may include a bypass first line BL1 and bypass And may be connected to the second line BL2.

Specifically, when the vaporizing first heat exchanger 241b or the vaporizing second heat exchanger 251b malfunctions or the liquefied gas does not completely vaporize, or when the customer 30 liquefies When the gas can not be received, the heated liquefied gas flowing in the first line (L1) can be supplied through the first bypass line (BL1) and the heated liquefied gas supplied from the bypass first line (BL1) Can exchange heat with the liquefied gas supplied through the first line (L1) from the buffer tank (22), and return the heat-exchanged liquefied gas to the buffer tank (22) through the second bypass line (BL2) have.

As described above, the first heat exchanger 27a is configured such that when the vaporization first heat exchanger 241b or the vaporization second heat exchanger 251b malfunctions or the liquefied gas does not completely vaporize, The heated liquefied gas flowing through the first line (L1) is supplied through the bypass first line (BL1) and heat-exchanged to re-liquefy even if the liquefied gas regeneration system (2) is not stopped , The driving reliability of the liquefied gas regeneration system 2 is improved, and the ability to cope with the system in an emergency situation is improved.

The liquefier 28 is provided between the first heat exchanger 27a and the buffer tank 22 on the second bypass line BL2 and is capable of expanding or reducing the liquefied gas heat-exchanged in the first heat exchanger 27a And can be re-liquefied by decompression. Here, the liquefier 28 may be an expander (preferably an expander) or a pressure reducer (preferably a line-Thomson valve).

In the present invention, since the bypassed liquefied gas returns to the buffer tank 22, the buffer tank 22 is not required to be a high-pressure vessel, and thus the construction cost of the buffer tank 22 is reduced , The vaporized liquefied gas is re-liquefied and supplied, so that the rise of the internal pressure of the buffer tank 22 can be effectively prevented.

Further, the liquefier 28 reduces or expands the bypassed liquefied gas and supplies it to the buffer tank 22, so that the inflow pressure to the second pump 23 can be kept constant. That is, the liquefier 28 adjusts the pressure of the bypassed liquefied gas and supplies it to the buffer tank 22, so that the effective suction head of the second pump 23 can be effectively satisfied.

As described above, in the embodiment of the present invention, since the liquefied gas heated (or vaporized) through the liquefier 28 is re-liquefied, it is not necessary to separately provide the evaporative gas compressor necessary for treating the vaporized liquefied gas, And the system is simplified.

The gas combustion apparatus 40 is supplied with the evaporation gas generated in the liquefied gas storage tank 10 through the second line L2 and the evaporation gas generated in the buffer tank 22 through the fourth line L4 It can burn.

As described above, in the liquefied gas regeneration system 2 according to the second embodiment of the present invention, an indirect vaporization method using steam and a direct vaporization method of steam are applied, and the direct vaporized steam is again supplied to the pre- (Heat exchanger 27a), it is possible to diversify vaporized fruits, thereby optimizing the operation cost of vaporization and improving driving reliability through various vaporization routes. In addition, And the driving stability is improved.

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

3, the liquefied gas regeneration system 3 according to the third embodiment of the present invention includes a liquefied gas storage tank 10, a first pump 21, a buffer tank 22, A second heat exchanger 291, a gas-liquid separator 292, a gas-liquid separator 292, and a gas-liquid separator 292. The pump 23, the vaporization first heat exchanger 241b, the vaporization second heat exchanger 251b, the first heat exchanger 27a, And a customer (30).

The configurations other than the first heat exchanger 27a, the liquefier 28, the second heat exchanger 291 and the gas-liquid separator 292 in the third embodiment of the present invention are the same as those in the first and second embodiments of the present invention The same reference numerals are used for the respective constructions and convenience, but they are not necessarily construed to refer to the same constructions.

The vessel equipped with the liquefied gas regeneration system 3 here is provided with a liquefied gas carrier line (not shown) for re-liquefying the liquefied gas at sea and supplying the liquefied gas to the land terminal, A liquefied gas regasification vessel (LNG RV) or a floating liquefied gas storage and regasification facility (FSRU) with the system 2 installed therein.

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

The embodiment of the present invention may further include a bypass third line BL3 instead of the bypass second line BL2. Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The bypass third line BL3 may include a liquefier 28 and a second heat exchanger 291 connecting the first heat exchanger 27a and the gas-liquid separator 292, and the first heat exchanger The bypassed liquefied gas heat-exchanged in the second heat exchanger 29a is heat-exchanged with the evaporated gas in the second heat exchanger 291, and then supplied to the gas-liquid separator 292. [

In the embodiment of the present invention, the seventh to ninth lines (L7 to L9) may further be included, and the configuration of the second line (L2) may be changed. Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The second line L2 may connect the liquefied gas storage tank 10 and the gas-liquid separator 292 and may include a second heat exchanger 291. The second line L2 may be connected to the gas- Exchanged with the bypassed liquefied gas supplied from the first heat exchanger (27a) in the second heat exchanger (291).

The seventh line L7 may connect the buffer tank 22 and the second line L2 and directly connect the second heat exchanger 292 and the buffer tank 22. [ The seventh line L7 can supply the gaseous liquefied gas generated or separated in the buffer tank 22 to the second line L2 or the second heat exchanger 291. [

The eighth line L8 connects the gas-liquid separator 292 and the second line L2. The gas separated from the gas-liquid separator 292 is supplied again to the second line L2, To return only the complete liquid to the liquefied gas storage tank (10).

The ninth line L9 can connect the gas-liquid separator 292 and the liquefied gas storage tank 10 and return the liquid separated in the gas-liquid separator 292 to the liquefied gas storage tank 10 again.

The first heat exchanger 27a supplies the bypassed liquefied gas heat-exchanged to the gas-liquid separator 292, unlike the second embodiment of the present invention in which the heat exchanged bypassed liquefied gas is returned to the buffer tank 22 , Except for the points described above, are the same as those described in the second embodiment of the present invention, so that the detailed contents are replaced with those described in the second embodiment of the present invention.

Unlike the second embodiment of the present invention in which the liquefied gas heat-exchanged in the first heat exchanger 27a is returned to the buffer tank 22, the liquefier 28 liquefies the liquefied gas heat-exchanged in the first heat exchanger 27a Is supplied to the gas-liquid separator 292 and is provided on the bypass third line BL3 instead of the bypass second line BL2. In addition to the above-described points, the description of the second embodiment of the present invention Therefore, the detailed contents are replaced with the contents described in the second embodiment of the present invention.

The second heat exchanger 291 is provided between the gas-liquid separator 292 and the first heat exchanger 27a on the third bypass line BL3 and is connected to the liquefied gas storage tank 10 on the second line L2. Liquid separator 292 and is supplied with the low-temperature liquefied gas re-liquefied through the first heat exchanger 27a and the liquefier 28 through the third line BL3, L2 to the evaporation gas generated in the liquefied gas storage tank 10 to exchange heat.

Specifically, the second heat exchanger 291 receives the liquefied gas re-liquefied through the first heat exchanger 27a and the liquefier 28 through the third line BL3 of the bypass line, The evaporated gas supplied through the second line L2 and re-liquefied can be supplied to the gas-liquid separator 292 through the second line L2, The liquefied gas supplied through the line BL3 and heat-exchanged with the evaporated gas supplied through the second line L2 may be supplied to the gas-liquid separator 292 through the third bypass line Bl3.

At this time, the evaporated gas supplied through the second line L2 may be a gas generated in the buffer tank 22 or the gas-liquid separator 292, as well as the liquefied gas storage tank 10.

The second heat exchanger 291 re-liquefies the evaporated gas generated in the liquefied gas storage tank 10 and supplies it to the gas-liquid separator 292. The second heat exchanger 291 is heat exchanged in the first heat exchanger 27a, It is possible to supply the re-liquefied bypass liquefied gas to the gas-liquid separator, so that the evaporation gas can be processed without the need for a separate compressor or a separate re-liquefying device, and a gas burning device is not necessary, , The system is greatly simplified and the driving reliability is improved.

Liquid separator 292 separates the liquefied gas re-liquefied from the second heat exchanger 291 through the bypass third line BL3 and the second line L2 into a gas phase and a liquid phase, Is supplied again to the second line (L2) through the eighth line (L8) or supplied again to the second heat exchanger (291), and the separated liquid phase flows through the ninth line (L9) to the liquefied gas storage tank Can be returned.

As described above, in the liquefied gas regeneration system 3 according to the third embodiment of the present invention, an indirect vaporization method using steam and a direct vaporization method of steam are applied, and the direct vaporized steam is again supplied to the pre- (Heat exchanger 27a), it is possible to diversify vaporized fruits, thereby optimizing the operation cost of vaporization and improving driving reliability through various vaporization routes. In addition, And the driving stability is improved.

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

4, the liquefied gas regeneration system 4 according to the fourth embodiment of the present invention includes a liquefied gas storage tank 10, a first pump 21, a buffer tank 22, The pump 23, the vaporization first heat exchanger 241a, the vaporization second heat exchanger 251a, the first heat exchanger 27b, the liquefier 28, the gas combustion device 40 and the suction device 70 .

The configurations other than the first heat exchanger 27a and the suction device 70 in the fourth embodiment of the present invention are the same as those of the first to third embodiments of the present invention, ≪ / RTI >

The vessel equipped with the liquefied gas regeneration system 4 here is provided with a liquefied gas carrier line (not shown) for re-liquefying the liquefied gas at sea and supplying the liquefied gas to the land terminal, May be a liquefied gas regasification vessel (LNG RV) or a floating liquefied gas storage and regasification facility (FSRU) with the system (4) installed therein.

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

In the embodiment of the present invention, the tenth to thirteenth lines L10 to L13 may further be included. Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The tenth line L10 may be branched between the vaporization first heat exchanger 241a and the vaporization second heat exchanger 251a on the first line L1 and connected to a suction device 70 to be described later, The liquefied gas vaporized in the first heat exchanger 241a may be supplied to the suction device 70 so that the liquefied gas vaporized in the vaporized first heat exchanger 241a may be used as the driving fluid for the suction device 70. [

The eleventh line L11 may be branched between the gas combustion device 40 on the second line L2 and the liquefied gas storage tank 10 and connected to the suction device 70, It is possible to discharge at least a part of the evaporated gas generated in the liquefied gas storage tank 10 to the suction device 70.

The twelfth line L12 may connect the suction device 70 and the first heat exchanger 27b and supply the evaporated gas discharged by the suction device 70 to the first heat exchanger 27b .

The thirteenth line L13 may include a liquefier 28 which connects the first heat exchanger 27b and the buffer tank 22 and is heat exchanged in the first heat exchanger 27b and is connected to the liquefier 28. [ So that the re-liquefied evaporated gas can be supplied to the buffer tank 22.

The first heat exchanger 27b may be provided between the second pump 23 and the vaporization first heat exchanger 241a on the first line L1 and may be provided between the twelfth line L12 and the thirteenth line L13).

Specifically, the first heat exchanger 27b evaporates through the twelfth line L12 by the suction device 70 when the amount of evaporated gas generated in the liquefied gas storage tank 10 is equal to or greater than a predetermined value, And the evaporated gas supplied from the twelfth line L12 can be exchanged with the liquefied gas supplied from the buffer tank 22 through the first line L1 and the heat exchanged evaporated gas can be supplied to the thirteenth And can be returned to the buffer tank 22 through the line L13.

The first heat exchanger 27b is configured to store the liquefied gas in the liquefied gas storage tank 10 when the amount of the evaporated gas generated by the liquefied gas storage tank 10 is equal to or greater than a preset value or the evaporated gas generated in the liquefied gas storage tank 10 It is possible to effectively manage the internal pressure of the liquefied gas storage tank 10 and to prevent the system 10 from being deteriorated when the internal pressure of the tank 10 rises above a predetermined value, And the construction cost can be minimized.

Also, the liquefied gas supplied to the vaporized first heat exchanger 241a by the second pump 23 can be preheated through the evaporated gas generated in the liquefied gas storage tank 10, so that the vaporized first heat exchanger 241a, And the vaporization second heat exchanger 251a can be reduced in size, thereby reducing the size of the vaporization first heat exchanger 241a and the vaporization second heat exchanger 251a, .

When the amount of evaporated gas generated in the liquefied gas storage tank 10 is equal to or larger than a predetermined value or when the evaporated gas generated in the liquefied gas storage tank 10 is introduced into the liquefied gas storage tank 10, The vaporized liquefied gas supplied from the vaporizing first heat exchanger 241a through the tenth line L10 is used as the driving fluid to cause the liquid fuel vapor generated in the liquefied gas storage tank 10 The evaporation gas can be discharged.

Of course, the suction device 70 is not limited to the tenth line L10 but also to the vaporization second heat exchanger 251a through a line (not shown) branched between the vaporization second heat exchanger 251a and the customer 30, The evaporated gas generated in the liquefied gas storage tank 10 can be discharged using the vaporized liquefied gas supplied from the liquefied gas storage tank 10 as a driving fluid.

The suction device 70 can suck the discharged evaporated gas through the eleventh line L11 and the sucked evaporated gas flows along with the driving fluid through the twelfth line L12 to the first heat exchanger 27b Can be supplied.

Here, the suction device 70 supplies the calculated amount of the driving fluid to the tenth line L10 through the vaporizing first heat exchanger 241a to suck all the evaporated gas generated in the liquefied gas storage tank 10 Can receive.

The suction device 70 is supplied with the liquefied gas vaporized by the driving fluid and sucks the evaporated gas generated in the liquefied gas storage tank 10 to mix the vaporized liquefied gas as the driving fluid with the evaporated gas, The kinetic energy of the mixed fluid is converted into the kinetic energy of the whole mixed fluid and then the kinetic energy of the mixed fluid decreases as the velocity of the mixed fluid at the end portion of the nozzle (not shown) Is again converted to pressure. Thus, the evaporated gas generated in the liquefied gas storage tank 10 is supplied to the first heat exchanger 27b in a pressurized state, and the pressurized evaporated gas is supplied through the first heat exchanger 27b and the liquefier 28 Can be re-liquefied.

Since the heat exchange and the depressurization or expansion occur in the state where the evaporation gas is pressurized when the liquid is re-liquefied, the effect of re-liquefaction can be obtained incidentally, and the effect of being pressurized by the suction device 70 can be obtained There is no need to construct a separate evaporative gas compressor, thereby reducing the construction cost and reducing the construction space, thereby enabling optimization of the ship space.

Here, the suction device 70 may be an ejector, an electric actuator, or a jet pump.

As described above, the liquefied gas regeneration system 4 according to the present invention is provided with the suction device 70 instead of the compressor in order to regenerate the BOG generated during regeneration, thereby reducing the construction cost and reducing the power consumption And the driving reliability can be improved because the failure rate is very small.

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

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

1 to 4: liquefied gas regeneration system of the first to fourth embodiments 10: liquefied gas storage tank
21: first pump 22: buffer tank
23: second pump 241a, b: vaporized first heat exchanger
242a, b: first vaporization heat exchanger 243a, b: first vaporization heat transfer pump
244: first vaporized fruit first control valve
245: first vaporization second control valve 251a, b: vaporization second heat exchanger
252a; Second vaporization heat exchanger 261: Second vaporization heat supply pump
262: second vaporization distributor 27a, b: first heat exchanger
28: liquefier 291: second heat exchanger
292: gas-liquid separator 30: customer
40: Evaporation gas demand place 51: Purging device
52: purge first control device 53: purge second control device
54: temporary storage tank 60: gas detection device
70: Suction device 80: Heater
L1 to L13: lines 1 to 13 SL1 to SL3: sea water lines 1 to 3
HL: Heating line GL: Glycol water line
ST1 to ST3: Steam first to third lines BL1 to 3: Bypass first to third lines

Claims (10)

A vaporizer for vaporizing the liquefied gas stored in the liquefied gas storage tank;
A heat exchanger for exchanging heat between the liquefied gas discharged from the vaporizing unit and returned at least partially to the liquefied gas supplied from the liquefied gas storage tank; And
And a liquefier for liquefying or liquefying the liquefied gas discharged from the vaporizing unit and heat-exchanged in the heat exchanger. The method according to claim 1,
A first pump for supplying liquefied gas stored in the liquefied gas storage tank;
A temporary storage tank for temporarily storing the liquefied gas supplied from the first pump; And
Further comprising a second pump for pressurizing the liquefied gas supplied from said temporary storage tank,
Wherein the vaporizing unit comprises:
A first vaporizer for primarily liquefying the liquefied gas supplied by the first pump with the first vaporized liquid; And
And a second vaporizer for delivering a heat source to the first vaporized fruit or direct secondary vaporization of the liquefied gas. 3. The method of claim 2,
Further comprising a gas combustion device for combusting the evaporated gas in which the liquefied gas is evaporated by thermal impregnation. 3. The apparatus according to claim 2, wherein the gas liquefied in the liquefier comprises:
And the liquid is supplied to the temporary storage tank. The apparatus of claim 3, wherein the temporary storage tank comprises:
The liquefied gas supplied from the liquefier and the liquefied gas supplied from the liquefied gas storage tank are mixed to separate into a liquid phase and a gaseous phase, the liquid phase is supplied to the second pump, and the gas phase is supplied to the gas combustion device And the liquefied gas regeneration system. The method according to claim 1,
The heat exchanger is a first heat exchanger,
A second heat exchanger for exchanging heat between the evaporated gas generated in the liquefied gas storage tank and the liquefied gas in the liquefier;
Further comprising a gas-liquid separator for separating the evaporated gas heat-exchanged in the second heat exchanger and the liquefied gas into a liquid phase and a gaseous phase. The method according to claim 6,
Wherein the evaporated gas supplied from the liquefied gas storage tank to the second heat exchanger is combined with the gas separated from the temporary storage tank or the gas separated from the gas-liquid separator and supplied to the second heat exchanger. Fire system. 8. The gas-liquid separator according to claim 7,
The separated gas is merged with the vaporized gas supplied from the liquefied gas storage tank to the second heat exchanger, and the separated liquid is returned to the liquefied gas storage tank. The method according to claim 1,
When at least a part or the whole amount of the liquefied gas vaporized by the vaporizing section is supplied to the heat exchanger when a demanding consumer consuming the liquefied gas vaporized by the vaporizing section malfunctions or the amount accommodated by the demanding consumer is not less than a preset capacity Characterized in that the liquefied gas regeneration system comprises: The method according to claim 1,
Wherein the heat exchanger is supplied with the entire amount of the fluid discharged from the vaporizing portion when the vaporizing portion malfunctions.

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