KR102373565B1 - A Regasification System Of Gas and Vessel having same - Google Patents

Abstract

Gas regasification system according to the present invention, a vaporizer for supplying the liquefied gas stored in the liquefied gas storage tank to regasification to a consumer; and a heat source supply device for transferring a heat source circulating while accompanied by a phase change to the vaporizer, wherein the heat source supply device includes an impurity removal device for increasing the purity of the heat source.

Description

A gas regasification system and a vessel including the same {A Regasification System Of Gas and Vessel having same}

The present invention relates to a gas regasification system and a ship including the same.

In general, LNG is a clean fuel and is known to have more abundant reserves than petroleum, and its usage is rapidly increasing as mining and transport technologies are developed. In such LNG, methane, the main component, is generally stored in a liquid state by lowering the temperature to -162 ° C or less under 1 atm. The volume of liquefied methane is about 1/600 of the volume of gaseous methane, which is a standard state, and the specific gravity is 0.42, which is about one-half of the share of crude oil.

LNG is liquefied due to its ease of transport and vaporized at the place of use after transport. However, there are concerns about installing LNG gasification facilities onshore due to the risk of natural disasters and terrorism.

For this reason, instead of the conventional liquefied natural gas regasification system installed on land, a regasification device is installed in an LNG carrier that transports liquefied natural gas and a facility to supply vaporized natural gas to land is in the spotlight.

In the LNG regasification system, the LNG stored in the liquefied gas storage tank is pressurized by the boosting pump and sent to the LNG vaporizer, and is vaporized to NG in the LNG vaporizer and sent to the demand on land. Here, a lot of energy is required in the process of heat exchange to increase the temperature of the LNG on the LNG vaporizer. Therefore, in order to solve the problem that energy used in this process is wasted due to inefficient exchange, various heat exchange technologies for efficient regasification are being studied.

The present invention was created to improve the prior art, and to provide a gas regasification system in which the regasification efficiency of liquefied gas can be maximized and a ship including the same.

Gas regasification system according to the present invention, a vaporizer for supplying the liquefied gas stored in the liquefied gas storage tank to regasification to a consumer; and a heat source supply device for transferring a heat source circulating while accompanied by a phase change to the vaporizer, wherein the heat source supply device includes an impurity removal device for increasing the purity of the heat source.

Specifically, the heat source supply device may include: a heat source circulation line circulating the heat source and having the vaporization device; a heat source storage tank provided on the heat source circulation line and storing the heat source; a heat source pump provided on the heat source circulation line and circulating the heat source; and a heat source vaporizer for vaporizing the heat source, wherein the impurity removal device may be provided between the heat source vaporizer and the vaporizer on the heat source circulation line.

Specifically, in the impurity removal device, a portion connected to the heat source circulation line may be provided on the upper side so that a heat source from which impurities are removed is supplied to the vaporization device, and a line for discharging the impurities to the outside may be provided on the lower side .

Specifically, the impurity removal device may discharge C4 or higher oil, solid impurities, and moisture among the impurities to the outside.

Specifically, the vaporizer may include: a vaporizer for vaporizing the liquefied gas; and a heater for heating the vaporized liquefied gas, wherein the heat source supply device circulates the heat source, the heat source circulation line having the vaporizer and the heater; a heat source storage tank provided on the heat source circulation line and configured to store the heat source supplied from the vaporizer; a heat source pump provided on the heat source circulation line and circulating the heat source supplied from the heat source storage tank; a heat source preheater preheating the heat source supplied from the heat source pump and supplying it to the heater; and a heat source vaporizer that vaporizes the liquid heat source supplied from the heater and supplies it to the vaporizer, wherein the impurity removal device may be provided between the heat source vaporizer and the vaporizer on the heat source circulation line.

Specifically, the heat source may be propane.

Specifically, a liquefied gas supply line connecting the liquefied gas storage tank and the customer; a feeding pump provided on the liquefied gas supply line and supplying the liquefied gas stored in the liquefied gas storage tank to the customer; a suction drum for temporarily storing the liquefied gas supplied from the feeding pump; and a boosting pump that receives the liquefied gas from the suction drum and pressurizes it to a high pressure to supply it to the vaporizer.

Specifically, a boil-off gas compressor for pressurizing the boil-off gas generated in the liquefied gas storage tank; and a power generation engine receiving the pressurized BOG from the BOG compressor to generate electric power.

Specifically, it may be a vessel comprising the gas regasification system.

A gas regasification system and a ship including the same according to the present invention have the effect that the regasification efficiency of liquefied gas can be maximized.

1 is a conceptual diagram of a ship having a gas regasification system according to an embodiment of the present invention.
2 is a conceptual diagram of a vaporizer of a conventional gas regasification system.
3 is a conceptual diagram of a vaporizer of a gas regasification system according to an embodiment of the present invention.
4 is a view showing a problem occurring inside the propane tank in the vaporizer of the conventional gas regasification system.

The objects, specific advantages and novel features of the present invention will become more apparent from the following detailed description and preferred embodiments taken in conjunction with the accompanying drawings. In the present specification, in adding reference numbers to the components of each drawing, it should be noted that only the same components are given the same number as possible even though they are indicated on different drawings. In addition, in describing the present invention, if it is determined that a detailed description of a related known technology may unnecessarily obscure the gist of the present invention, the detailed description thereof will be omitted.

Hereinafter, in this specification, liquefied gas may be used to encompass all gas fuels that are generally stored in a liquid state, such as LNG or LPG, ethylene, ammonia, etc. can be expressed as This can be applied to boil-off gas as well. In addition, for convenience, LNG may be used to encompass both NG (Natural Gas) in a liquid state as well as NG in a supercritical state, etc. can

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 ship having a gas regasification system according to an embodiment of the present invention.

As shown in Figure 1, the conventional gas regasification system (1), a liquefied gas storage tank (10), a feeding pump (20), a boosting pump (21), a suction drum (30), a vaporizer (40) , including a boil-off gas compressor 50 , a first demand source 61 , and a second demand source 62 .

Here, the ship (symbol not shown) in which the gas regasification system 1 is installed has a hull (H) composed of a bow part (symbol not shown), a stern part (symbol not shown), and an upper deck (symbol not shown). The propeller shaft (S) is propelled by transmitting the power produced by the engine (E) of the engine room (symbol not shown) disposed in the stern portion to the propeller (P) and operating.

In addition, the ship regasifies liquefied gas in which a gas regasification system 1 is installed on a liquefied gas carrier (not shown) in order to regasify the liquefied gas at sea and supply the liquefied gas to an onshore terminal. It can be a vessel (LNG RV) or a floating liquefied gas storage and regasification facility (FSRU).

Hereinafter, a gas regasification system 1 according to an embodiment of the present invention will be described with reference to FIG. 1 .

The gas regasification system 1 according to the embodiment of the present invention extracts liquefied gas in a liquid state from the liquefied gas storage tank 10 through the feeding pump 20 and passes through the suction drum 30 to the boosting pump 21 . After pressurizing to the furnace, the vaporizer 40 heats the liquefied gas through a heat source to regasify it, and a method of supplying it to the first consumer 61 is used. That is, in simple terms, the gas regasification system 1 of the present invention regasifies the liquefied gas using the vaporizer 40 and supplies it to the first consumer 61 . At this time, the BOG generated in the liquefied gas storage tank 10 was pressurized by the BOG compressor 50 and supplied to the second consumer 62 for treatment.

The vaporizer 40 may receive seawater directly from the seawater supply device (not shown) and regasify the liquefied gas (direct regasification method), and receive seawater indirectly from the seawater supply device to regas the liquefied gas. (Indirect regasification method; a method in which propane, an intermediate fruit, is supplied with a heat source of seawater from the propane vaporizer 434, and propane supplies the heat source supplied from the seawater to the vaporizer 40 again. )

All embodiments of the present invention will be described based on the indirect regasification method, and it should be noted that this is only for convenience of description and is not specifically limited in the present invention.

Before describing the individual components of the gas regasification system 1 according to the embodiment of the present invention, basic flow paths for organically connecting the individual components will be described. Here, the flow path is a passage through which the fluid flows and may be a line.

In the embodiment of the present invention, the liquefied gas first supply line (L1), the liquefied gas second supply line (L2), may further include a boil-off gas supply line (L3). Valves (not shown) capable of adjusting the opening degree may be installed in each line, and the supply amount of boil-off gas or liquefied gas may be controlled according to the control of the opening degree of each valve.

The liquefied gas first supply line L1 connects the liquefied gas storage tank 10 and the suction drum 30 and includes a feeding pump 20 to feed the liquefied gas stored in the liquefied gas storage tank 10 . It can be supplied to the suction drum 30 through (20). In this case, the liquefied gas first supply line L1 may be connected to the suction drum 30 and at the same time branch from the upstream of the suction drum 30 and directly connected to the liquefied gas second supply line L2 .

The liquefied gas second supply line (L2) connects the suction drum 30 and the first consumer 61 and includes a boosting pump 21 and a vaporizer 40, and the liquefied gas temporarily stored in the suction drum 30 The gas or liquefied gas directly supplied from the first supply line L1 may be pressurized by the boosting pump 21 and re-vaporized by the vaporizer 40 to be supplied to the first consumer 61 .

The boil-off gas supply line (L3) connects the liquefied gas storage tank 10 and the second demand source 62, and includes a boil-off gas compressor 50 to collect the boil-off gas generated from the liquefied gas storage tank 10. It can be supplied to the second consumer 62 by pressurizing the boil-off gas compressor (50).

Hereinafter, individual components that are organically formed by each of the above-described lines L1 to L3 to implement the gas regasification system 1 will be described.

The liquefied gas storage tank 10 stores the liquefied gas to be supplied to the first consumer 61 . The liquefied gas storage tank 10 should store the liquefied gas in a liquid state. At this time, the liquefied gas storage tank 10 may have a pressure tank shape.

Here, the liquefied gas storage tank 10 is disposed inside the hull (H), and may be formed in four, for example, in front of the engine room. In addition, the liquefied gas storage tank 10 is, for example, a membrane type tank, but is not limited thereto, and the type is not particularly limited to various types, such as an independent tank.

The feeding pump 20 is provided on the liquefied gas first supply line L1, is installed inside or outside the liquefied gas storage tank 10, and liquefies the liquefied gas stored in the liquefied gas storage tank 10 to a suction drum ( 30) can be supplied.

Specifically, the feeding pump 20 is provided between the liquefied gas storage tank 10 and the suction drum 30 on the liquefied gas first supply line L1 to supply the liquefied gas stored in the liquefied gas storage tank 10 . It may be supplied to the suction drum 30 by primary pressure.

The feeding pump 20 may supply the suction drum 30 by pressurizing the liquefied gas stored in the liquefied gas storage tank 10 to 6 to 8 bar. Here, the feeding pump 20 may pressurize the liquefied gas discharged from the liquefied gas storage tank 10 to slightly increase the pressure and temperature, and the pressurized liquefied gas may still be in a liquid state.

At this time, the feeding pump 20 may be a submersible pump when provided inside the liquefied gas storage tank 10 , and stored in the liquefied gas storage tank 10 when installed outside the liquefied gas storage tank 10 . It may be provided at a position inside the hull (H) lower than the level of the liquefied gas and may be a centrifugal pump.

The boosting pump 21 may be provided between the suction drum 30 and the vaporizer 40 on the liquefied gas second supply line L2, and the liquefied gas or the suction drum supplied from the feeding pump 20 ( 30) may be supplied to the vaporizer 40 by pressurizing the liquefied gas supplied from 80 to 120 bar.

The boosting pump 21 may pressurize the liquefied gas according to the pressure required by the first demand 61 , and may be configured as a centrifugal pump.

The suction drum 30 may be connected to the liquefied gas first supply line L1 to receive the liquefied gas from the liquefied gas storage tank 10 and temporarily store it.

Specifically, the suction drum 30 may receive the liquefied gas stored in the liquefied gas storage tank 10 from the feeding pump 20 through the liquefied gas first supply line L1, and temporarily use the supplied liquefied gas. By storing, the liquefied gas may be separated into a liquid phase and a gas phase, and the separated liquid may be supplied to the boosting pump 21 .

That is, the suction drum 30 temporarily stores the liquefied gas, separates the liquid phase and the gas phase, and then supplies the complete liquid to the boosting pump 21 so that the boosting pump 21 satisfies the effective suction head (NPSH). , thereby preventing cavitation in the boosting pump 21 .

The vaporizer 40 may be provided on the liquefied gas second supply line L2 to regasify the high-pressure liquefied gas discharged from the boosting pump 21 .

Specifically, the vaporizer 40 is provided on the liquefied gas second supply line L2 between the first demand source 61 and the boosting pump 21 and is composed of a vaporizer 41 and a heater 42, boosting After vaporizing the high-pressure liquefied gas supplied from the pump 21 through the vaporizer 41 , the first consumer 61 may heat it to a desired temperature through the heater 42 and supply it to the first consumer 61 .

Hereinafter, the conventional vaporizer 40a will be described in detail with reference to FIG. 2 .

2 is a conceptual diagram of a vaporizer of a conventional gas regasification system.

As shown in FIG. 2 , the vaporizer 40a of the conventional gas regasification system receives an intermediate fruit (the first heat medium) through a heat source circulation line L4 and exchanges heat with the liquefied gas to vaporize the liquefied gas and , the high-pressure vaporized liquefied gas can be supplied to the first consumer 61 without pressure fluctuation. Here, the intermediate fruit heat-exchanged with the liquefied gas is circulated again through the heat source circulation line L4.

As an intermediate fruit in the conventional vaporizer 40a, propane is used, and in this case, the purity of propane must be ultra-high purity.

If the purity of the propane used in the conventional vaporizer 40a is not sufficient, heavy hydrocarbon accumulates in the form of droplets or solids with high viscosity on the heat source circulation line L4 through which propane circulates. As a result, there was a problem in that the performance of the conventional vaporizer 40a was lowered or, worse, the entire regasification system was shut down (Shut Down).

Accordingly, the conventional vaporizer 40a cannot continuously operate the regasification system, and has to stop the operation of the conventional vaporizer 40a for maintenance, thereby significantly increasing the operating cost.

In addition, there are frequent cases in which solid impurities generated during the manufacturing process and pre-drive test process in the equipment and heat source circulation line L4 of the conventional vaporizer 40a cannot be completely removed before operation of the conventional vaporizer 40a. Accordingly, there was also a problem in that solid impurities were accumulated in the heat source circulation line L4, thereby lowering the driving efficiency of the system. (Referring to (a), (b), (c), and (d) of FIG. 4 , it can be seen that a large amount of solid impurities generated at the inlet of the propane tank 431 are present.)

In order to solve the above problems, the present applicant has developed a vaporizer 40b of the present invention, which will be described in detail below with reference to FIG. 3 .

Reference numerals 431, 432, 433, and 434 not described in FIG. 2 are a propane tank 431, a propane pump 432, a propane preheater 433, and a propane vaporizer 434, respectively, and in FIG. 3, the vaporizer of the present invention ( 40b) will be described in detail.

3 is a conceptual diagram of a vaporizer of a gas regasification system according to an embodiment of the present invention.

3, the vaporizer 40b of the gas regasification system 1 according to the embodiment of the present invention is a vaporizer 41, a heater 42, a heat source circulation line L4, a propane tank ( 431 ), a propane pump 432 , a propane preheater 433 , a propane vaporizer 434 , and an impurity removal device 435 .

Here, the vaporizer 40b may be referred to as a heat source supply device except for the vaporizer 41 and the heater 42, and supplies heat to the vaporizer 41 or the heater 42, and a heat source circulation line (L4) Propane may be used as a heat source that circulates. Of course, here, the heat source is not limited to propane, and any heat source that circulates while accompanied by a phase change may be included.

The heat source circulation line L4 includes a vaporizer 41, a heater 42, a propane tank 431, a propane pump 432, a propane preheater 433, a propane vaporizer 434, and an impurity removal device 435. and a propane tank 431 , a propane pump 432 , a propane preheater 433 , a heater 42 , a propane vaporizer 434 , an impurity removal device 435 , and a vaporizer 41 .

The propane tank 431 is provided between the propane pump 432 and the vaporizer 41 on the heat source circulation line L4 and may store propane circulating the heat source circulation line L4.

The propane tank 431 may store liquid propane, and may take the form of a pressure vessel.

The propane pump 432 is provided between the propane tank 431 and the propane preheater 433 on the heat source circulation line L4, and may circulate propane on the heat source circulation line L4.

The propane pump 432 may receive liquid propane from the propane tank 431 and supply it to the propane preheater 433 , and may supply it under pressure of about 70 bar.

Here, the propane pump 432 may be a centrifugal pump.

The propane preheater 433 is provided between the propane pump 432 and the heater 42 on the heat source circulation line L4, and after preheating the liquid propane supplied from the propane pump 432 to approximately 25 degrees, the heater 42 ) can be supplied.

In this case, the propane preheater 433 does not cause a phase change of propane, and can supply propane having a pressure of about 70 bar supplied from the propane pump 432 to the heater 42 without a pressure change.

The propane preheater 433 may use steam or seawater as a preheating heat source, and may share a heat source with the propane vaporizer 434 .

The propane vaporizer 434 is provided between the heater 42 and the impurity removal device 435 on the heat source circulation line L4, and is supplied with liquid propane having an approximate room temperature of 9 degrees supplied from the heater 42 to receive gas can be vaporized with

The propane vaporizer 434 may vaporize propane into a gas and supply it to the impurity removal device 435 . Here, the propane vaporizer 434 may use steam or sea water as a vaporization heat source, and may share a heat source with the propane preheater 433 .

The impurity removal device 435 is provided between the propane vaporizer 434 and the vaporizer 41 on the heat source circulation line L4 to remove propane and impurities inherent in the equipment, thereby increasing the purity of propane.

The impurity removal device 435 removes impurities (moisture, C4 or higher oil, solid impurities (sand, iron powder, etc.)) inherent in propane using gravity, and collects impurities at the lower side and high-purity propane at the upper side can do.

Accordingly, the impurity removal device 435 is connected to the heat source circulation line L4 so that the propane from which impurities have been removed is supplied to the vaporizer 41 on the upper side, and is connected to a line for discharging the impurities removed from the lower side to the outside. .

Here, the impurity removal device 435 may drain C4 or higher oil and moisture (water) out of the impurities.

A component in propane that causes the above-described problems (accumulation of droplets in the pipe, accumulation of solid impurities, etc.) in the vaporizer 40b is C4 plus heavy hydrocarbon. Therefore, the impurity removal device 435 can remove the impurities by adopting the method of removing the impurities by gravity.

A result table for predicting the change in the purity of propane after using the impurity removal device 435 is shown below.

Prediction of propane purity change after using the impurity removal device 435 (calculation, simulation)
initial
(no separator) After installing the impurities removal device (435) initial vapor=97.41% initial vapor=95% initial vapor=90% propane molarity 97.41% 99.51% 99.78% 99.85% C4 plus molarity 0.72% 0.31% 0.1% 0.04% C4 plus removal rate (%) - 56.94% 86.11% 94.44%

As described in the table above, when the initial propane molar concentration is 97.41%, the purity change of propane is improved to 99.51% after the impurity removal device 435 is installed and driven. At this time, the C4 plus removal rate reached 56.41%.

In addition, the C4 plus removal rate is higher as the initial propane concentration is lower. When the initial propane molar concentration is 95%, it is possible to produce propane with high purity up to 99.78%, in this case the removal rate approaches 86.11%, and when the initial propane molar concentration is 90%, propane with high purity up to 99.85% , and in this case, the removal rate approaches 94.44%.

As described above, in the vaporizer 40b according to the embodiment of the present invention, the impurity removal device 435 is provided on the heat source circulation line L4, so that impurities can be removed without stopping the system, so that the performance of the system is improved. Drive stability is increased, and system reliability is maximized.

In addition, in the vaporizer 40b according to the embodiment of the present invention, the impurity removal device 435 is disposed between the vaporizer 41 and the propane vaporizer 434 to remove the vaporized propane and immediately produce high-purity propane. Since it can be supplied to the vaporizer 41, it is very easy to remove impurities and has the effect of dramatically improving the vaporization rate.

In addition, since the vaporizer 40b according to the embodiment of the present invention includes the impurity removal unit 435, the purity of propane can be improved along with driving, so high-purity propane can not be used, and the vaporizer ( 40b) has the effect of reducing the driving cost.

The boil-off gas compressor 50 may pressurize the boil-off gas generated in the liquefied gas storage tank 10 and supply it to the second consumer 62 .

Specifically, the boil-off gas compressor 50 is provided on the boil-off gas supply line L3 and pressurizes the boil-off gas generated in the liquefied gas storage tank 10 to about 6 to 8 bar or 6 to 15 bar to the second consumer ( 62) can be supplied.

A plurality of BOG compressors 50 may be provided to pressurize BOG in multiple stages, and for example, three BOG compressors 50 may be provided to pressurize BOG in three stages. The three-stage compressor exemplified herein is merely an example and is not limited to the three-stage compressor.

In an embodiment of the present invention, a boil-off gas cooler (not shown) may be provided at each rear end of the boil-off gas compressor 50 . When the boil-off gas is pressurized by the boil-off gas compressor 50, the temperature of the boil-off gas may be lowered again by using the boil-off gas cooler in the present embodiment because the temperature may also increase as the pressure rises. The BOG cooler may be installed in the same number as the BOG compressor 50 , and each BOG cooler may be provided downstream of each BOG compressor 50 .

In addition, in the embodiment of the present invention, when the boil-off gas compressor 50 is provided in parallel to rapidly increase the amount of boil-off gas generated in the liquefied gas storage tank 10, all of them can be accommodated, or the boil-off gas compressor When one of (50) malfunctions or is shut down (Shut down), the other BOG compressor (50) can operate to efficiently receive and process BOG generated in the liquefied gas storage tank (10). can

The first consumer 61 may receive and consume the liquefied gas vaporized by the vaporizer 40 . Here, the first demand 61 may be used by supplying gaseous liquefied gas by vaporizing liquefied gas, and may be a land terminal installed on land or an offshore terminal installed floating on the sea.

The second consumer 62 receives the boil-off gas generated from the liquefied gas storage tank 10 and uses it as fuel. That is, the second consumer 62 requires boil-off gas and may be driven by using it as a raw material. The second demand 62 may be a generator (eg, DFDG), a gas combustion unit (GCU), or a boiler (eg, a boiler generating steam), but is not limited thereto.

Specifically, the second consumer 62 is connected to the boil-off gas supply line L3 to receive boil-off gas, and the boil-off gas pressurized to a low pressure of about 1 to 6 bar (maximum 15 bar) by the boil-off gas compressor 50 is supplied. It can be supplied and used as fuel.

In addition, the second consumer 62 may be a heterogeneous fuel engine capable of using different fuels, so that not only BOG but also oil can be used as fuel, but BOG and oil are not mixed and supplied, BOG or oil is optional can be supplied as This is to prevent the two materials having different combustion temperatures from being mixed and supplied, thereby preventing the efficiency of the second consumer 62 from falling.

Here, the second consumer 62 may be provided on the deck (not shown) of the engine room provided inside the stern.

As described above, the ship having the gas regasification system 1 according to the present invention has the effect that the regasification efficiency of the liquefied gas can be maximized.

Although the present invention has been described in detail through specific examples, it is intended to describe the present invention in detail, and the present invention is not limited thereto, and by those of ordinary skill in the art within the technical spirit of the present invention It will be clear that the transformation or improvement is possible.

All simple modifications or changes of the present invention fall within the scope of the present invention, and the specific scope of protection of the present invention will be made clear by the appended claims.

1: Ship 10: Liquefied Gas Storage Tank
20: feeding pump 21: boosting pump
30: suction drum 40: vaporizer
40a: conventional vaporizer 40b: vaporizer of the present invention
431: propane tank 432: propane pump
433: propane preheater 434: propane vaporizer
435: impurity removal device 41: vaporizer
42: heater 50: boil-off gas compressor
61: first consumer 62: second consumer
L1: Liquefied gas first supply line L2: Liquefied gas second supply line
L3: BOG supply line L4: Heat source circulation line
E: propulsion engine S: propeller shaft
P: propeller H: hull

Claims (9)

a vaporizer for re-vaporizing the liquefied gas stored in the liquefied gas storage tank and supplying it to a consumer; and
A heat source supply device for transferring a circulating heat source to the vaporizer while accompanied by a phase change,
The heat source supply device,
and an impurity removal device for increasing the purity of the heat source,
The vaporizer is
a vaporizer for vaporizing the liquefied gas; and
A heater for heating the vaporized liquefied gas,
The heat source supply device,
a heat source circulation line circulating a heat source and having the vaporizer and the heater;
a heat source pump provided on the heat source circulation line and circulating the heat source;
a heat source preheater preheating the heat source supplied from the heat source pump and supplying it to the heater;
and a heat source vaporizer that vaporizes the liquid heat source supplied from the heater and supplies it to the vaporizer,
The impurity removal device,
Gas regasification system, characterized in that provided between the heat source vaporizer and the vaporizer on the heat source circulation line. According to claim 1, wherein the heat source supply device,
Gas regasification system provided on the heat source circulation line, further comprising a heat source storage tank for storing the heat source. According to claim 2, wherein the impurity removal device,
Gas regasification system, characterized in that the portion connected to the heat source circulation line is provided on the upper side so that the heat source from which impurities are removed is supplied to the vaporization device, and the line for discharging the impurities to the outside is provided on the lower side. According to claim 3, wherein the impurity removal device,
Gas regasification system, characterized in that for discharging C4 or higher oil, solid impurities, and moisture among the impurities to the outside. delete According to claim 1, wherein the heat source,
Gas regasification system, characterized in that propane (Propane). The method of claim 1,
a liquefied gas supply line connecting the liquefied gas storage tank and the customer;
a feeding pump provided on the liquefied gas supply line and supplying the liquefied gas stored in the liquefied gas storage tank to the consumer;
a suction drum for temporarily storing the liquefied gas supplied from the feeding pump; and
Gas regasification system, characterized in that it receives the liquefied gas from the suction drum and pressurizes it to a high pressure, further comprising a boosting pump for supplying the liquefied gas to the vaporizer. 8. The method of claim 7,
BOG compressor for pressurizing BOG generated in the liquefied gas storage tank; and
Gas regasification system, characterized in that it further comprises a power generation engine for generating power by receiving the boil-off gas pressurized from the boil-off gas compressor. 9. The method according to any one of claims 1 to 4, 6 to 8,
and said gas regasification system.

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