KR20200028252A - Liquefied gas re-gasification system - Google Patents

Abstract

According to one embodiment of the present invention, provided is a liquefied gas re-gasification system. According to one embodiment of the present invention, the liquefied gas re-gasification system comprises: a gas supply line which supplies liquefied gas stored in a storage tank; a pressurizing pump which is installed in the gas supply line, and pressurizes the liquefied gas; a carburetor which is installed in the gas supply line on a rear end of the pressurizing pump, and gasifies the pressurized liquefied gas into evaporated gas by exchanging heat with a heat medium; a first circulation line which constitutes an independent cycle to allow the heat medium to circulate, and passes through the carburetor; a first heater which is installed in the first circulation line, exchanges heat of the heat medium cooled by passing through the carburetor with the heat of steam, and heats up to a first temperature; a circulation pump which is installed in the first circulation line between the carburetor and the first heaters, and pressurizes the heat medium; a second circulation line which constitutes an independent cycle, allows steam to circulate, and passes through the circulation pump and the first heaters in order; and a boiler which is installed in the second circulation line, and gasifies the steam which is liquefied by passing through the first heaters. The circulation pump can be driven by the energy of the steam. The present invention aims to provide the liquefied gas re-gasification system which can reduce power consumption for driving the system, and improve the efficiency of the system.

Description

Liquefied gas re-gasification system

The present invention relates to a liquefied gas regasification system, and more particularly, to a liquefied gas regasification system capable of improving system efficiency by reducing the amount of power consumed to drive the system.

In general, liquefied natural gas (LNG: Liquefied Natural Gas) cools natural gas to cryogenic and about -163 ° C, significantly reducing its volume, LNG carriers, floating storage and re-floating storage (FSRU) -gasification unit). However, liquefied natural gas is stored in a liquid tank in a storage tank of an LNG carrier or a floating liquefied gas storage vessel, and a consumer who consumes liquefied natural gas usually consumes liquefied natural gas in a gaseous state rather than in a liquid state. It is necessary to regasify the gas before supplying it to the consumer. Therefore, LNG carriers, floating liquefied gas storage vessels, and the like are provided with a regasification system for evaporating cryogenic liquefied natural gas with heat medium such as seawater and engine waste heat to vaporize with high temperature and high pressure evaporation gas.

On the other hand, since the liquefied natural gas in the liquid state is a cryogenic state of about -163 ° C, when the temperature difference with the heat medium during the heat exchange is too large, the durability of the heat exchanger heating the liquefied natural gas may decrease, and liquefied natural using seawater Direct heating of the gas can cause corrosion in the heat exchanger. Accordingly, to reduce the temperature difference between the liquefied natural gas and the heating medium, a regasification system has been developed in which glycol water is used as a heating medium, and heat exchange between liquefied natural gas and sea water is performed to indirectly heat the liquefied natural gas. However, such a regasification system, there is a problem that the pump for pressurizing the heating medium and the pump for pressurizing sea water are driven by an electric motor to increase the power consumption and decrease the system efficiency.

Accordingly, there is a need for a liquefied gas regasification system that can improve system efficiency by reducing the amount of power consumed to drive the system.

Republic of Korea Registered Patent No. 10-0609350 (July 28, 2006)

The technical problem to be achieved by the present invention is to provide a liquefied gas regasification system capable of improving system efficiency by reducing the amount of power consumed to drive the system.

The technical problems of the present invention are not limited to the technical problems mentioned above, and other technical problems not mentioned will be clearly understood by those skilled in the art from the following description.

A liquefied gas regasification system according to an embodiment of the present invention for achieving the above technical problem is a gas supply line for supplying liquefied gas stored in a storage tank, and a pressure installed on the gas supply line to pressurize the liquefied gas A pump and a vaporizer installed on the gas supply line at the rear end of the pressurized pump to exchange the pressurized liquefied gas with a heat medium to vaporize the vaporized gas into an evaporation gas, and an independent cycle to circulate the heat medium and pass through the vaporizer 1 circulation line, a first heater installed on the first circulation line to heat the heat medium cooled by passing through the vaporizer with steam, and heating to a first temperature; and the agent between the vaporizer and the first heater. A circulation pump installed in a circulation line to pressurize the heat medium, and an independent cycle to circulate the steam, and the circulation A second circulation line passing through the first heater and the first heater in turn, and a boiler installed on the second circulation line to vaporize the vapor liquefied while passing through the first heater, wherein the circulation pump includes the steam Is powered by energy.

The liquefied gas regasification system is installed on the gas supply line at the rear end of the vaporizer to heat the evaporated gas with the heating medium and heat it to a temperature required by a consumer, and the first circulation at the rear end of the first heater A second heater installed on a line to heat the heating medium heated to the first temperature to a second temperature required by the vaporizer, and branched from the first circulation line at the rear end of the second heater to pass through the auxiliary heater A first branch line may be further included, and the first branch line may be joined to the first circulation line at the rear end of the vaporizer.

The liquefied gas regasification system. In the sea water supply line for supplying the sea water, passing through the second heater, a sea water pump installed in the sea water supply line before the second heater to pressurize the sea water, and the second circulation line at the rear end of the boiler Branching, further comprising a second branch line joined to the second circulation line before the first heater after passing through the sea water pump, the sea water pump may be driven by the energy of the steam.

The heat medium may be glycol water, which is a mixture of ethylene glycol and water.

The liquefied gas regasification system is installed on the gas supply line between the storage tank and the pressurized pump, and may further include a liquefied gas drum in which the liquefied gas is temporarily stored.

The liquefied gas regasification system may further include a bypass line branched from the gas supply line between the pressurized pump and the vaporizer and connected to the liquefied gas drum.

According to the present invention, since the circulation pump for pressurizing the heating medium and the seawater pump for pressing the seawater are respectively driven using the energy of steam heating the heating medium, the amount of power consumed for driving the system can be reduced to improve system efficiency. .

In addition, since it can be implemented by simply adding piping in a regasification system using conventional glycol water and seawater, it can be easily applied to existing LNG carriers, floating liquefied gas storage vessels, and the like.

1 is a view showing a liquefied gas regasification system according to an embodiment of the present invention.
2 is an operation diagram for explaining the operation of the liquefied gas regasification system.

Advantages and features of the present invention, and methods for achieving them will be clarified with reference to embodiments described below in detail together with the accompanying drawings. However, the present invention is not limited to the embodiments disclosed below, but may be implemented in various different forms, and only the embodiments allow the disclosure of the present invention to be complete, and common knowledge in the art to which the present invention pertains It is provided to completely inform the person having the scope of the invention, and the present invention is only defined by the scope of the claims. The same reference numerals refer to the same components throughout the specification.

Hereinafter, a liquefied gas regasification system according to an embodiment of the present invention will be described in detail with reference to FIGS. 1 and 2.

The liquefied gas regasification system according to an embodiment of the present invention is a device that vaporizes liquefied natural gas into high temperature and high pressure evaporated gas through heat exchange between a cryogenic liquefied natural gas and a heat medium, and supplies it to a consumer on land, for example, LNG It can be installed on ships or offshore structures such as carriers, floating liquefied gas storage vessels, and the like.

The liquefied gas regasification system drives a circulation pump that pressurizes the heating medium and a seawater pump that pressurizes the seawater, respectively, by using the energy of steam heating the heating medium, thereby reducing the amount of power consumed to drive the system and improving system efficiency. have. In addition, since it can be implemented by simply adding piping in a regasification system using conventional glycol water and seawater, it has a feature that can be easily applied to existing LNG carriers, floating liquefied gas storage vessels, and the like.

Hereinafter, the liquefied gas regasification system 1 will be described in detail with reference to FIG. 1.

1 is a view showing a liquefied gas regasification system according to an embodiment of the present invention.

The liquefied gas regasification system 1 according to the present invention includes a gas supply line 10, a pressurized pump 20, a vaporizer 30, a first circulation line 40, and a first heater 50. , A circulation pump 60, a second circulation line 70, and a boiler 80.

The gas supply line 10 is a line for supplying liquefied gas stored in a storage tank (not shown), one end of which is connected to the lower portion of the storage tank and the other end is extended to directly consume or indirectly to a consumer, for example, a consumer on land. Can be connected to. Here, the liquefied gas is a gas liquefied by cooling or compressing a gaseous compound or mixture, and may be, for example, Liquefied Natural Gas (LNG). Hereinafter, the liquefied gas is limited to the liquefied natural gas and will be described in more detail. Liquefied gas is supplied to the gas supply line 10 in a state of -161.3 ° C, 5.5 bar, and moves to the pressurized pump 20 along the gas supply line 10.

The pressurized pump 20 is installed on the gas supply line 10 to pressurize the liquefied gas, and may be a conventional high pressure booster pump. The pressurized pump 20 may pressurize the liquefied gas to a pressure or higher required by the consumer, and the liquefied gas passing through the pressurized pump 20 may be in a state of -155 ° C and 111.3 bar. In the drawing, although one pressure pump 20 is illustrated as being installed on the gas supply line 10, the present invention is not limited thereto, and a plurality of pressure pumps 20 may be installed in series to pressurize the liquefied gas in multiple stages. . A liquefied gas drum 11 for temporarily storing liquefied gas and discharging it at a constant pressure is installed in the gas supply line 10 between the storage tank and the pressurized pump 20, and a fixed amount of liquefied gas is provided in the pressurized pump 20. It can be supplied at a constant pressure.

The liquefied gas drum 11 separates the liquefied gas from the gas phase and the liquefied gas from the liquid phase to condense the liquefied gas from the gas phase, and the internal pressure may be maintained higher than the internal pressure of the gas supply line 10. That is, the liquefied gas drum 11 may simultaneously function as a buffer tank, a separator, and a re-condenser. The liquefied gas drum 11 may have a bypass line 12 connected to one side. The bypass line 12 is a line branched from the gas supply line 10 between the pressurized pump 20 and the vaporizer 30 to be described later, and may be connected to the upper side of the liquefied gas drum 11. By bypassing the bypass line 12 on the gas supply line 10, an amount of liquefied gas corresponding to the design capacity of the vaporizer 30 can be supplied to the vaporizer 30 along the gas supply line 10, Due to this, the vaporization efficiency of the vaporizer 30 can be maximized. In addition, the remaining amount of liquefied gas exceeding the design capacity of the vaporizer 30 may be supplied to the liquefied gas drum 11 along the bypass line 12, so that the internal pressure of the liquefied gas drum 11 is a gas supply line. It can be maintained higher than the internal pressure of (10). The liquefied gas flowing through the bypass line 12 is pressurized in the pressurized pump 20, so even if there is no separate pumping device for pressurizing the liquefied gas on the bypass line 12, the liquefied gas is used as the liquefied gas drum 11 Supply can be made smoothly. In addition, by maintaining the internal pressure of the liquefied gas drum 11 higher than the internal pressure of the gas supply line 10, the liquefied gas can be discharged at a constant pressure to the pressure pump 20. On the bypass line 12 and the gas supply line 10 at the rear end of the bypass line 12, a valve for controlling the flow of liquefied gas is installed, and the flow of liquefied gas and the gas supply line 10 on the bypass line 12 side are provided. ) You can control the flow of liquefied gas on the side.

The vaporizer 30 is installed on the gas supply line 10 at the rear end of the pressurized pump 20 to heat the liquefied gas pressurized by the pressurized pump 20 with a heat medium to vaporize with evaporated gas, and may be a normal heat exchanger. Here, the heat medium is a mixture of at least two different substances, and may be, for example, glycol water, which is a mixture of ethylene glycol and water. When glycol water is used as a heating medium, there is a small risk of corrosion of a heat exchanger or a pipe line, it is safe because it is not explosive, and it is easy to change the composition. However, the heating medium is not limited to being glycol water, and the heating medium can be variously modified. The liquefied gas in the liquid state receives heat through heat exchange with the heat medium in the vaporizer 30 and vaporizes it into a gaseous evaporation gas, and the high temperature and high pressure heat medium loses heat through heat exchange with the liquefied gas to become a low temperature and low pressure state. For example, -155 ℃, 111.3bar liquefied gas is vaporized through heat exchange with 15 ℃, 1.5bar heat medium in the vaporizer 30 to become -15 ℃, 110bar evaporation gas, and the heat medium is -8 ℃, 0.5 It can be cooled to bar. As described above, since the liquefied gas is pressurized in the pressurized pump 20, it can be easily vaporized through heat exchange with the heat medium, and cooling energy due to latent heat of evaporation generated when the liquefied gas is vaporized is absorbed by the heat medium. You can. The heat medium may pass through the vaporizer 30 through the first circulation line 40 to be described later, and may circulate the first circulation line 40 while absorbing cooling energy. The first circulation line 40 will be described in more detail below. The evaporated gas generated by the vaporization of the liquefied gas moves to the auxiliary heater 31 installed in the gas supply line 10 at the rear end of the vaporizer 30.

The auxiliary heater 31 is to heat the boil-off gas to the heat medium by heating with a heat medium, and may be a normal heat exchanger. For example, the evaporation gas of -15 ° C and 110bar heats up with the heat medium of 15 ° C and 1.5bar in the auxiliary heater 31 to become 5 ° C and 100bar, and the heat medium can be cooled to 0 ° C and 0.5bar. . At this time, the heating medium may pass through the auxiliary heater 31 through the first branch line 41 branched from the first circulation line 40, and the first branch line 41 will be described in more detail below. do. The boiled gas heated in the auxiliary heater 31 is supplied to the consumer in a state of 5 ° C. and 100 bar through the gas supply line 10.

On the other hand, as described above, the heat medium circulates the first circulation line 40 while absorbing cooling energy. The first circulation line 40 constitutes an independent cycle, and is a line through which the heat medium circulates, and may pass through the vaporizer 30. More specifically, a circulation pump 60, a first heater 50, and a second heater 51 are sequentially installed on the first circulation line 40, and the vaporizer 30 is disposed at the rear end of the second heater 51. Via.

The first heater 50 passes through the vaporizer 30 and heats the cooled heat medium with steam to heat to a first temperature, and may be a normal heat exchanger. Here, the first temperature may be a temperature required to maximize the heat exchange efficiency between the heat medium and seawater in the second heater 51 to be described later, and the steam is produced through the second circulation line 70 to be described later. 1 may pass through the heater 50. The heat medium cooled by passing through the vaporizer 30 receives heat through heat exchange with steam in the first heater 50 and is heated to a first temperature, and high-temperature and high-pressure steam loses heat through heat exchange with the heat medium to liquefy. Can be. At least one circulation pump 60 is installed in the first circulation line 40 between the carburetor 30 and the first heater 50, and the circulation pump 60 is a heat medium for circulating the first circulation line 40 Can be pressed. For example, the heat medium passed through the vaporizer 30 and cooled to -8 ° C and 0.5 bar is pressurized by the circulation pump 60 to a state of -6.13 ° C and 5bar, and a first state of -6.13 ° C and 5bar. The heater 50 is heated through heat exchange with -0.67 bar, 585 kcal / kg of steam, and may be in a state of 5 ° C and 4 bar. The second heater 51 is installed in the first circulation line 40 at the rear end of the first heater 50. The second heater 51 heats the heat medium and seawater heated at the first temperature to the first heater 50 and heats it to the second temperature required by the vaporizer 30, and may be a normal heat exchanger. For example, the heat medium heated to the first temperature receives heat through heat exchange with seawater at 14 ° C. or lower in the second heater 51 to become 15 ° C., 1.5 bar, and sea water heats through heat exchange with the heat medium. It can be lost to 7 ℃. Sea water is supplied through the sea water supply line 90, and the sea water supply line 90 is connected to the sea or the sea water storage tank (not shown), and the other side via the second heater 51 to the sea or It can be connected to a seawater storage tank. At least one seawater pump 91 that pressurizes the seawater may be installed in the seawater supply line 90 at the front end of the second heater 51.

In addition, a heating medium supply line 100 may be connected to one side of the first circulation line 40, more specifically, the first circulation line 40 between the vaporizer 30 and the circulation pump 60. The heating medium supply line 100 is a line for supplying the heating medium to the first circulation line 40, one side of which is connected to the heating medium storage tank 110 and the other side of which is connected to the first circulation line 40. The heating medium storage tank 110 is a tank for storing the heating medium, and may be stored in a mixture state by mixing ethylene glycol and water in an appropriate ratio, or separately storing ethylene glycol and water. When the heating medium storage tank 110 separates and stores ethylene glycol and water, the heating medium storage tank 110 or the heating medium supply line 100 is provided with a separate mixing device capable of mixing ethylene glycol and water in an appropriate ratio. Can be. The heat medium supply line 100 may be opened when the system is initially operated, or may be opened when the ethylene glycol ratio of the heat medium circulating through the first circulation line 40 is lowered or the water ratio is increased. When the heat medium supply line 100 is opened, the ethylene glycol ratio of the heat medium circulating in the first circulation line 40 becomes high, so that the freezing point of the heat medium decreases, so that the heat medium freezes during heat exchange with liquefied gas in the vaporizer 30. Can be prevented.

Meanwhile, the first branch line 41 is branched to the first circulation line 40 at the rear end of the second heater 51, and the first branch line 41 is rear end of the vaporizer 30 via the auxiliary heater 31. It may be joined to the first circulation line (40). That is, the heating medium of 15 ° C and 1.5 bar heated by the second heater 51 partially moves along the first circulation line 40 to pass through the vaporizer 30, and the remaining part of the first branch line 41. After moving along the auxiliary heater 31, it is joined to the first circulation line 40 at the rear end of the carburetor 30. The first branch line 41 is branched from the first circulation line 40 and passed through the auxiliary heater 31 to vaporize the liquefied gas by using the heating medium heated in the second heater 51 and to simultaneously evaporate gas. Since it can be heated, there is an advantage that a single heating medium can be used in various ways.

The second circulation line 70 constitutes an independent cycle, and is a line through which steam circulates. The second circulation line 70 may sequentially pass through the circulation pump 60 and the first heater 50. More specifically, the feed pump 81 and the boiler 80 are sequentially installed on the second circulation line 70 and pass through the circulation pump 60 and the first heater 50 in turn at the rear end of the boiler 80.

The boiler 80 passes through the first heater 50 to vaporize the liquefied vapor, and may be a conventional boiler. The vapor liquefied by heat exchange with the heat medium in the first heater (50) is pressurized through the feed pump (81) and moves to the boiler (80), heated by the boiler (80) and vaporized to pass through the circulation pump (60). You can. For example, the liquid vapor that has passed through the first heater 50 may be -0.67 bar, 69.5 kcal / kg, and is pressurized by the feed pump 81 to become a state of 16 bar, 69.5 kcal / kg, followed by a boiler. Heated at 80, it can be 14.5bar, 667kcal / kg of steam. 14.5bar, 667kcal / kg of steam generated in the boiler 80 passes through the circulation pump 60, the circulation pump 60 can be driven with the energy of the steam, thereby driving the circulation pump 60 System efficiency may be improved by reducing the amount of power consumed in the system. In the conventional case in which the circulation pump 60 is driven by an electric motor, there is a problem in that the system efficiency is low due to large power consumption. However, since the present invention uses the enthalpy of steam generated in the boiler 80 as a power source for the circulation pump 60, the amount of power consumed to drive the system can be reduced to improve system efficiency. The steam that has passed through the circulation pump 60 passes through the first heater 50 in a state of -0.67 bar, 585 kcal / kg, and the enthalpy of steam is transferred to the heating medium in the first heater 50, so that the heating medium is the first. It can be heated to temperature.

The second branch line 71 is branched to the second circulation line 70 at the rear end of the boiler 80. The second branch line 71 is branched from the second circulation line 70 between the boiler 80 and the circulation pump 60, and after passing through the seawater pump 91, the second of the front end of the first heater 50 It may be joined to the circulation line 70. That is, 14.5bar, 667kcal / kg of steam generated in the boiler 80 is partially moved along the second circulation line 70 to pass through the circulation pump 60, and the other part is the second branch line 71 It moves along and passes through the seawater pump 91 and then joins the second circulation line 70 before the first heater 50. The steam generated in the boiler 80 moves along the second branch line 71 and passes through the sea water pump 91, whereby the sea water pump 91 can be driven with the energy of the steam, and thereby, the sea water pump ( The amount of power consumed for driving 91) may be reduced to improve system efficiency. In the conventional case where the seawater pump 91 is driven by an electric motor, there is a problem that the power consumption is large and the system efficiency is low. However, since the present invention uses the enthalpy of steam generated in the boiler 80 as a power source for the seawater pump 91, the amount of power consumed to drive the system can be reduced to improve system efficiency. The steam that has passed through the seawater pump 91 becomes -0.67 bar, 585 kcal / kg, passes through the first heater 50 after joining the second circulation line 70.

Hereinafter, the operation of the liquefied gas regasification system will be described in more detail with reference to FIG. 2.

2 is an operation diagram for explaining the operation of the liquefied gas regasification system.

The liquefied gas regasification system 1 according to the present invention drives the system by driving the circulation pump 60 that pressurizes the heat medium by using the energy of the steam heating the heat medium, and the seawater pump 91 that pressurizes the seawater, respectively. The amount of power consumed in the system can be reduced to improve system efficiency. In addition, since it can be implemented by simply adding piping in a regasification system using conventional glycol water and seawater, it can be easily applied to existing LNG carriers, floating liquefied gas storage vessels, and the like.

The liquefied gas stored in the storage tank is supplied to the liquefied gas drum 11 through the gas supply line 10 and discharged at a constant pressure from the liquefied gas drum 11 to move to the pressurized pump 20. The pressurized pump 20 pressurizes the liquefied gas to a pressure or higher required by the consumer, and the pressurized liquefied gas is vaporized by evaporating gas by exchanging heat with the heat medium circulating in the first circulation line 40 in the vaporizer 30. . At this time, only the amount corresponding to the design capacity of the vaporizer 30 among the liquefied gas pressurized by the pressure pump 20 is supplied to the vaporizer 30 through the gas supply line 10, and the rest through the bypass line 12 Return to the liquefied gas drum (11). The vaporized gas generated in the vaporizer 30 moves to the auxiliary heater 31 along the gas supply line 10, and is exchanged with the heat medium that flows through the first branch line 41 in the auxiliary heater 31 to be required by the consumer. After being heated to the desired temperature, it is supplied to the consumer.

On the other hand, the heat medium circulating in the first circulation line 40 is cooled by heat exchange with liquefied gas in the vaporizer 30, and is introduced into the first heater 50 after being pressurized by the circulation pump 60. The first heater 50 heats the cooled and pressurized heat medium with steam circulating in the second circulation line 70 to heat to a first temperature, and the heat medium heated to the first temperature is seawater from the second heater 51. The heat is exchanged with seawater supplied through the supply line 90 to be heated to a second temperature. The heating medium heated in the second heater 51 partially moves along the first circulation line 40 and passes through the vaporizer 30, and the remaining part moves along the first branch line 41 to assist the heater 31. ) And then join the first circulation line 40 at the rear end of the vaporizer 30.

The steam circulating in the second circulation line 70 is liquefied by heat-exchanging with the heat medium in the first heater 50, and is introduced into the boiler 80 after being pressurized by the feed pump 81. Boiler 80 is vaporized by heating the liquefied steam, the steam generated in the boiler 80 is partially moved to the circulation pump 60 along the second circulation line 70 to drive the circulation pump 60 and , The remaining part moves to the seawater pump 91 along the second branch line 71 to drive the seawater pump 91. The steam that has passed through the circulation pump 60 and the steam that has passed through the seawater pump 91 are joined at the front end of the first heater 50 and pass through the first heater 50.

Although the embodiments of the present invention have been described with reference to the accompanying drawings, a person skilled in the art to which the present invention pertains may be implemented in other specific forms without changing the technical concept or essential features of the present invention. You will understand. Therefore, it should be understood that the embodiments described above are illustrative in all respects and not restrictive.

1: Liquefied gas regasification system
10: gas supply line 11: liquefied gas drum
12: bypass line 20: pressurized pump
30: carburetor 31: auxiliary heater
40: first circulation line 41: first branch line
50: first heater 51: second heater
60: circulation pump 70: second circulation line
71: second branch line 80: boiler
81: feed pump 90: seawater supply line
91: seawater pump 100: heating medium supply line
110: heat medium storage tank

Claims (6)

A gas supply line for supplying liquefied gas stored in a storage tank;
A pressure pump installed on the gas supply line to pressurize the liquefied gas;
A vaporizer installed on the gas supply line at the rear end of the pressurized pump to exchange the pressurized liquefied gas with a heat medium to vaporize the vaporized gas;
A first circulation line through which the heat medium is circulated by configuring an independent cycle and passing through the vaporizer;
A first heater installed on the first circulation line to heat the heat medium cooled by passing through the carburetor with steam to heat to a first temperature;
A circulation pump installed in the first circulation line between the vaporizer and the first heater to pressurize the heat medium;
A second circulation line through which the steam circulates by configuring an independent cycle and sequentially passes through the circulation pump and the first heater; And
Is installed on the second circulation line includes a boiler to vaporize the vapor liquefied through the first heater,
The circulation pump is a liquefied gas regasification system driven by the energy of the steam. The auxiliary heater of claim 1, wherein the auxiliary heater is installed in the gas supply line at the rear end of the vaporizer to heat the evaporated gas with the heat medium to heat to a temperature required by the consumer.
A second heater installed on the first circulation line behind the first heater and heating the heat medium heated to the first temperature to a second temperature required by the vaporizer, and
Further comprising a first branch line branched from the first circulation line after the second heater via the auxiliary heater,
The first branch line is a liquefied gas regasification system joined to the first circulation line at the rear end of the vaporizer. According to claim 2, Supplying the sea water, and the sea water supply line via the second heater,
A seawater pump installed in the seawater supply line in front of the second heater to pressurize the seawater, and
The second branch line is branched from the second circulation line at the rear end of the boiler, and further comprises a second branch line joined to the second circulation line before the first heater after passing through the seawater pump,
The seawater pump is a liquefied gas regasification system driven by the energy of the steam. The liquefied gas regasification system according to claim 1, wherein the heat medium is glycol water, which is a mixture of ethylene glycol and water. The liquefied gas regasification system of claim 1, further comprising a liquefied gas drum installed in the gas supply line between the storage tank and the pressurized pump and temporarily storing the liquefied gas. The liquefied gas regasification system of claim 5, further comprising a bypass line branched from the gas supply line between the pressurized pump and the vaporizer and connected to the liquefied gas drum.

Images