CN116654184A - Ship with gas regasification system - Google Patents

Abstract

The ship with the gas regasification system of the present invention is characterized in that it includes: a hull; a vaporizer installed on the upper part of the hull, and the vaporizer vaporizes the liquefied gas and supplies it to a place where it is needed; and a heat source supply device is installed on the Inside the hull, the heat source supply device supplies a heat source to the vaporizer.

Description

Ships with gas regasification systems

This application is a divisional application of the patent application with the application number CN2017800090226, the application date is March 30, 2017, and the invention title is "ship with gas regasification system".

technical field

The invention relates to a ship with a gas regasification system.

Background technique

Generally, it is known that LNG is a clean fuel, and its reserves are also more abundant than petroleum. With the development of mining and transshipment technology, the use of LNG has also increased sharply. Such LNG is usually stored in a liquid state by lowering the temperature of methane as the main component to -162°C or lower at 1 atmosphere, and the volume of liquefied methane is about 1/600 of the volume of methane in the standard gas state. , with a specific gravity of 0.42, roughly 1/2 of that of crude oil.

LNG is liquefied and transported because of its ease of transport, and then vaporized at the point of use for use. However, there is concern about installing LNG vaporization facilities on land due to natural disasters and the risk of terrorism.

In this way, instead of the conventional LNG regasification system installed on land, a regasification device is installed on an LNG carrier carrying liquefied natural gas (Liquefied Natural Gas) to supply evaporated natural gas (Natural Gas) to land, and it has attracted attention.

In the LNG regasification device system, the LNG stored in the liquefied gas storage tank is pressurized by the booster pump and supplied to the LNG vaporizer, and then supplied to the land where needed after the LNG vaporizer is vaporized into NG. Here, a large amount of energy is required in the process of heat exchange to increase the temperature of LNG in the LNG evaporator. Therefore, various heat exchangers for efficient regasification are being researched in order to solve the waste problem caused by inefficient exchange of energy used in the process.

Contents of the invention

The problem to be solved by the invention

The present invention is made to improve the conventional technology, and an object of the present invention is to provide a ship having a gas regasification system capable of maximizing the regasification efficiency of liquefied gas.

Technical solution to the problem

The ship with the gas regasification system of the present invention is characterized in that it includes: a hull; a vaporizer installed on the upper part of the hull, and the vaporizer vaporizes the liquefied gas to supply it to a required place; and a heat source supply device is installed on the Inside the hull, the heat source supply device supplies a heat source to the vaporizer.

Specifically, at least one deck for dividing the interior space of the hull up and down is also included.

Specifically, the heat source supply device includes: a heat source pump for supplying the heat source, a seawater heat exchanger for exchanging heat between the heat source and seawater, and a heat source circulation line on which The heat source pump and the seawater heat exchanger; the heat source pump and the seawater heat exchanger are divided and arranged on the upper side or the lower side of each other by the deck.

Specifically, it further includes: a seawater pump for supplying the seawater to the seawater heat exchanger, and a seawater line, the seawater flows on the seawater line, and the seawater pump is arranged on the seawater line And the seawater heat exchanger; the diameter of the heat source circulation line is smaller than the diameter of the seawater line.

Specifically, one end of the seawater line is connected to a seawater inlet formed on the side of the hull, and the other end of the seawater line is connected to a seawater outlet formed on the side of the hull; the heat source supply device The area where the seawater discharge port is provided is arranged inside the hull.

Specifically, the seawater pump is arranged on the bow side inside the hull.

Specifically, it also includes a steam heat exchanger for exchanging heat between the heat source and steam; The lower side divides the configuration.

Specifically, it also includes: a boiler that generates the steam, the boiler is arranged in the engine room inside the hull, and a steam line connects the steam heat exchanger and the The boiler; at least a part of the steam line is provided inside a hull (Hull) formed at the bottom of the hull.

Specifically, after using the seawater, the steam is used to exchange heat with the heat source.

Specifically, the heat source supply device is made as a module including the heat source pump, the seawater heat exchanger or the steam heat exchanger.

Specifically, the heat source supply device is disposed on the bow side inside the hull.

Specifically, the heat source supply device is disposed on a side surface inside the hull.

Specifically, the heat source supply device is disposed on a side of an engine room disposed inside a stern of the hull.

Specifically, the heat source is a non-explosive refrigerant.

Specifically, the heat source is glycol water.

Specifically, the heat source supply device includes a pressure maintaining device for maintaining the pressure of the heat source flowing in the heat source circulation line; the pressure maintaining device maintains the pressure of the heat source by using an inert gas.

Invention effect

The ship with the gas regasification system of the present invention has the effect of maximizing the regasification efficiency of liquefied gas.

Description of drawings

FIG. 1 is a conceptual diagram of a ship having a gas regasification system according to a conventional embodiment.

Fig. 2 is a conceptual diagram of a ship with a gas regasification system according to an embodiment of the present invention.

Fig. 3 is a conceptual diagram showing a gas regasification system of another embodiment of the present invention.

FIG. 4 is a conceptual diagram showing a gas regasification system of an embodiment of the present invention.

Fig. 5 is a conceptual diagram of a ship with a gas regasification system according to still another embodiment of the present invention.

FIG. 6 is a conceptual diagram showing a gas regasification system according to still another embodiment of the present invention.

Fig. 7 is a conceptual diagram illustrating in detail a gas regasification system according to still another embodiment of the present invention.

Fig. 8 is a conceptual diagram showing a glycol water circulation device according to an embodiment of the present invention.

Fig. 9 is a conceptual diagram of a seawater supply device of the present invention.

Detailed ways

The objects, specific advantages and novel features of the present invention will become more apparent from the following detailed description and preferred embodiments in connection with the accompanying drawings. In this specification, when assigning reference numerals to structural members in each drawing, even if they appear in different drawings, the same reference numerals are assigned to the same structural members as much as possible. In addition, when describing the present invention, when it is judged that the specific description of related known technologies will obscure the gist of the present invention, the detailed description will be omitted.

In this specification below, liquefied gas can be used as a concept covering all gaseous fuels that are usually stored in a liquid state, such as LNG or LPG, ethylene, ammonia, etc., even if they are not in a liquid state due to heating or pressurization Inferior, also expressed as liquefied gas for convenience. The same applies to boil-off gases. In addition, for convenience, LNG can be used not only as a liquid state NG (Natural Gas) but also as a concept of NG in a supercritical state, etc., and boil-off gas can be used as not only a gaseous state of boil-off gas but also liquefied Evaporated gas concept.

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

FIG. 1 is a conceptual diagram of a ship having a gas regasification system according to a conventional embodiment.

As shown in FIG. 1 , a conventional gas regasification system 1 includes a liquefied gas storage tank 10 , a feed pump 20 , a buffer tank 30 , a vaporizer 40 and a place of need 70 .

In the conventional gas regasification system 1, the liquefied gas in a liquid state is extracted from the liquefied gas storage tank 10 by the feed pump 20 and sent to the booster pump 21 through the buffer tank 30, and the liquefied gas is extracted by the booster pump 21 After pressurization, the liquefied gas is heated by a heat source in the evaporator 40 to be re-evaporated, and then supplied to the place of need 70 .

In such a gas regasification system 1 , a plurality of liquefied gas storage tanks 10 are arranged inside the hull 100 , and on the other hand, the recondenser 30 , the booster pump 21 , and the carburetor 40 are arranged in the regasification unit room 1000. Driven internally, the regasification unit chamber 1000 is disposed on the upper side of the upper deck 104 of the bow 101 .

The disposition of multiple structures such as the recondenser 30, the booster pump 21, and the vaporizer 40 is because the composition of the liquefied gas is composed of explosive substances, so it is not installed inside the closed hull 100 with poor circulation to ensure safety. sex.

The evaporator 40 receives the first heat medium through the seawater heat exchanger 41 and the heat source pump 42 provided on the heat source circulation line L3 to re-evaporate the liquefied gas. Explosive refrigerants such as propane or butane are used as the first heat medium. Therefore, like the plurality of structures of the gas regasification system 1 , the structure of the seawater heat exchanger 41 and the heat source pump 42 that supply the heat source to the evaporator 40 are also arranged on the upper side of the upper deck 104 to be driven.

On the other hand, the seawater pump 51, which is a structure for supplying seawater to the seawater heat exchanger 41, can only be located in the engine room 51 according to the internal arrangement conditions of the hull 100, and thus is used to connect the seawater heat exchanger 41 and the seawater pump 51. The length of the sea line L4 becomes considerably longer. Compared with the heat source circulation line L3, the seawater line L4 has corrosion resistance, and a large amount of seawater needs to be supplied to the seawater heat exchanger 41, so there is a problem that the cost is relatively high.

In addition, as described above, due to the presence of an explosive refrigerant, the positions to be placed on the hull 100 are limited, and there is a problem that the space efficiency in the hull 100 is seriously impaired.

The present invention has been developed to solve such problems, and details thereof will be described below.

Unexplained reference signs L1, L2, 61, 102, 103, 105, H1, H2, E, S, P, ER, D are the liquefied gas supply line L1, the re-gasification line L2, the second demand place 61, Central part 102, stern part 103, ship bottom 105, seawater inflow H1, seawater outflow H2, engine E, propeller shaft S, propeller P, engine room ER, deck D, in the following Figures 2 to 4 In the embodiment of the present invention described in the description, detailed description is given.

Fig. 2 is a conceptual diagram of a ship with a gas regasification system according to an embodiment of the present invention.

As shown in Figure 2, the gas regasification system 2 of the embodiment of the present invention includes a liquefied gas storage tank 10, a feed pump 20, a booster pump 21, a buffer tank 30, a vaporizer 40, a second need place 61, a first need place 70 and a boil-off gas compressor 80.

For convenience, in the embodiment of the present invention, the liquefied gas storage tank 10, the feed pump 20, the booster pump 21, the buffer tank 30, the vaporizer 40, the second need place 61, the first need place 70, etc. use different The various structures of the gas regasification system 1 have the same reference numerals, but do not necessarily refer to the same structures.

Here, the ship provided with the gas regasification system 2 has a hull 100 consisting of a bow 101, a center 102, a stern 103, an upper deck 104, and a bottom 105, and the propeller shaft S will be arranged at the stern. The power generated by the engine E in the engine room ER of the section 103 is transmitted to the propeller P to operate, thereby propelling the ship.

In addition, the ship may be a liquefied gas regasification vessel (LNG RV) equipped with a gas regasification system 2 on a liquefied gas carrier (not marked with reference numerals), or a floating liquefied gas storage and regasification vessel. Gasification Unit (FSRU) to be able to supply the liquefied gas to an onshore terminal after regasification at sea.

Next, referring to FIG. 2 , the gas regasification system 2 according to the embodiment of the present invention will be described.

Before describing the individual structures of the gas regasification system 2 according to the embodiment of the present invention, a plurality of basic flow paths for organically connecting individual structures will be described. Here, the flow path may be a passage line (Line) through which fluid flows, but it is not limited thereto, as long as it is a structure that allows fluid to flow.

In the embodiment of the present invention, it may further include a liquefied gas supply line L1, a regasification line L2, a heat source circulation line L3, a seawater line L4, a steam line L5, a boil-off gas supply line L6 and a boil-off gas branch line L7. A plurality of valves (not shown) whose openings can be adjusted can be provided in each line, and the supply amount of boil-off gas or liquefied gas can be controlled by adjusting the openings of each valve.

The liquefied gas supply line L1 connects the liquefied gas storage tank 10 and the buffer tank 30 , and has a feed pump 20 , which can supply the liquefied gas stored in the liquefied gas storage tank 10 to the buffer tank 30 . At this time, the liquefied gas supply line L1 may be connected to the buffer tank 30 and branched from the upstream of the buffer tank 30 to be directly connected to the regasification line L2.

The regasification line L2 connects the buffer tank 30 to the first need point 70, and has a booster pump 21 and a vaporizer 40, which can temporarily store the liquefied gas in the buffer tank 30 or directly supply the liquefied gas from the liquefied gas supply line L1, After being pressurized by the booster pump 21 , it is re-gasified by the vaporizer 40 and supplied to the first demand place 70 .

The heat source circulation line L3 circulates and connects the evaporator 40, the seawater heat exchanger 41, and the heat source pump 42, thereby circulating the first heat medium to each structure. Here, the diameter of the heat source circulation line L3 may be smaller than the diameter of the seawater line L4.

In addition, with regard to the heat source circulation line L3, each heat source supply line L3 connected to the evaporator 40 (shown in FIGS. 6 and 7 ), the seawater heat exchanger 41 and the heat source pump 42 constituted by four skids is constituted as one. Common line. At this time, in the carburetor 40, a first carburetor skid 401 to a fourth carburetor skid 404 (shown in FIGS. ), the first skid-mounted block 401 to the fourth skid-mounted block 404 (shown in FIGS. 6 and 7 ) can be connected with the heat source supply lines L3a-L3d of the branches branched from the heat source supply line L3 (Fig. 6 and 7 shown in ) connection.

At this time, as far as the heat source supply line L3 is concerned, when the heat source supply line L3 configured as a common line penetrates the upper deck 104, only two are formed, which has the effect of improving the durability of the upper deck 104 of the bow 101 and reducing heat source leakage. Possibility, which has the effect of improving system reliability. In addition, the heat source supply line L3 can be configured as an additional line in parallel, thereby sufficiently securing the flow rate of glycol water that can be accommodated in one heat source supply line L3. In this case, the number of lines passing through the upper deck 104 of the bow 101 may be four.

The seawater line L4 connects the seawater inflow port H1 and the seawater outflow port H2 , and has a seawater pump 51 and a seawater heat exchanger 41 , and can supply seawater to the seawater heat exchanger 41 through the seawater pump 51 . Here, the diameter of the seawater line L4 may be larger than the diameter of the heat source circulation line L3, and a corrosion-resistant material may be coated inside the seawater line L4.

The steam line L5 connects the second demand point 61 and the steam heat exchanger 62 , and can supply the steam generated at the second demand point 61 to the steam heat exchanger 62 .

The boil-off gas supply line L6 connects the liquefied gas storage tank 10 and the buffer tank 30, and has a boil-off gas compressor 80, and can supply the boil-off gas generated by the liquefied gas storage tank 10 to the Buffer tank 30. At this time, the boil-off gas supply line L6 may be connected to the lower side of the buffer tank 30 .

The boil-off gas branch line L7 can be branched from the boil-off gas compressor 80 downstream on the boil-off gas supply line L6 to be connected to the second demand point 61, and the boil-off gas pressurized by the boil-off gas compressor 80 can be supplied to the second place. Office 61 is required.

Next, individual structures for realizing the gas regasification system 2 by organically forming the lines L1 to L7 described above will be described.

The liquefied gas storage tank 10 stores liquefied gas to be supplied to the first demand point 70 . The liquefied gas storage tank 10 needs to store the liquefied gas in a liquid state. In this case, the liquefied gas storage tank 10 may have a form of a pressure tank.

Here, the liquefied gas storage tank 10 is arranged inside the hull 100 , and as an example, four liquefied gas storage tanks 10 may be formed in front of the engine room. In addition, as an example, the liquefied gas storage tank 10 may be a membrane structure tank, but it is not limited thereto, and may be a tank of various forms such as an independent tank, and is not particularly limited.

As for the liquefied gas storage tanks 10 , a coffer dam 106 may be disposed between the respective liquefied gas storage tanks 10 , or a coffer dam 106 may be disposed between the engine room ER and the liquefied gas storage tank 10 .

The feed pump 20 is installed on the liquefied gas supply line L1 and can be installed inside or outside the liquefied gas storage tank 10 to supply the liquefied gas stored in the liquefied gas storage tank 10 to the buffer tank 30 .

Specifically, the feed pump 20 is installed between the liquefied gas storage tank 10 and the buffer tank 30 on the liquefied gas supply line L1, and can pressurize the liquefied gas stored in the liquefied gas storage tank 10 once and supply it to the buffer tank. 30.

The feed pump 20 can pressurize the liquefied gas stored in the liquefied gas storage tank 10 to 6 bar to 8 bar to supply it to the buffer tank 30 . Here, the feed pump 20 may pressurize the liquefied gas discharged from the liquefied gas storage tank 10 to slightly increase its pressure and temperature, and the pressurized liquefied gas may still be in a liquid state.

At this time, when the feed pump 20 is arranged inside the liquefied gas storage tank 10, the feed pump 20 may be a concealed pump, and when the feed pump 20 is arranged outside the liquefied gas storage tank 10, the feed pump 20 may be a concealed pump. The feed pump 20 may be installed at a position inside the hull H lower than the water level of the liquefied gas stored in the liquefied gas storage tank 10, and may be a centrifugal pump.

The booster pump 21 can be installed between the buffer tank 30 and the vaporizer 40 on the liquefied gas supply line L1, and can pressurize the liquefied gas supplied by the feed pump 20 or the liquefied gas supplied by the buffer tank 30 to 50 bar to 120 bar It is supplied to the vaporizer 40 .

The booster pump 21 can pressurize the liquefied gas according to the pressure required by the first demand place 70 , and the booster pump 21 can be a centrifugal pump. Here, the booster pump 21 may be provided on the upper side of the upper deck 104 of the bow 101 .

The buffer tank 30 can be connected to the liquefied gas supply line L1, and can receive the liquefied gas supplied by the liquefied gas storage tank 10 for temporary storage.

Specifically, the buffer tank 30 can receive the liquefied gas stored in the liquefied gas storage tank 10 from the feed pump 20 through the liquefied gas supply line L1, and temporarily store the supplied liquefied gas, thereby separating the liquefied gas into a liquid phase and a gas phase. , and the separated liquid phase is supplied to the booster pump 21 .

That is, the buffer tank 30 temporarily stores the liquefied gas and separates it into a liquid phase and a gas phase, and then supplies the complete liquid phase to the booster pump 21 so that the booster pump 21 satisfies the effective cavitation head (NPSH). Cavitation (cavitation) in the booster pump 21 is prevented.

In addition, the buffer tank 30 may be connected to the boil-off gas supply line L6 to receive the boil-off gas generated by the liquefied gas storage tank 10 for temporary storage.

Specifically, the buffer tank 30 may receive the boil-off gas generated by the liquefied gas storage tank 10 from the boil-off gas compressor 80 through the boil-off gas supply line L6 for temporary storage.

In this manner, the buffer tank 30 can perform recondensation by exchanging heat between the liquefied gas received from the liquefied gas supply line L1 and temporarily stored and the boil-off gas received from the boil-off gas supply line L6 and temporarily stored. Here, the buffer tank 30 may be formed as a pressure vessel type capable of withstanding a pressure of 6 to 8 bar or 6 to 15 bar.

Therefore, the buffer tank 30 receives the boil-off gas and the liquefied gas at a pressure of about 6 bar to 8 bar (or 6 bar to 15 bar) through the boil-off gas compressor 80 and the feed pump 20. Compared with the low-pressure boil-off gas or liquefied gas, the In order to improve the recondensation efficiency, recondensation is performed while maintaining the above-mentioned pressure, and the pressure is supplied to the booster pump 21, thereby reducing the compression load of the booster pump 21.

At this time, the buffer tank 30 may have a spraying part 31 and a filling part 32 to effectively recondense the temporarily stored liquefied gas and evaporated gas.

The spraying part 31 can be formed extending from the end of the liquefied gas supply line L1 to the inside of the buffer tank 30 , and is provided above the packing part 32 , and can spray the liquefied gas supplied through the liquefied gas supply line L1 to the packing part 32 .

The spraying part 31 can spray the liquefied gas in liquid phase to increase the contact area of the liquefied gas and the evaporating gas, and can perform a similar function to that of the packing part 32 .

The packing part 32 may be provided in the center of the inside of the buffer tank 30, and a member such as crushed stone may be formed inside the packing part 32 to expand the liquefied gas supplied to the liquefied gas supply line L1 and the liquefied gas supplied to the boil-off gas supply line L6. The surface area over which the supplied evaporative gases come into contact with each other. That is, the packing part 32 can form many voids by the gravel formed inside the packing part 32, and the liquefied gas can flow through the voids, thereby increasing the area in contact with the boil-off gas.

In this way, the filler part 32 can increase the heat exchange efficiency between the liquefied gas and the boil-off gas, thereby improving the recondensation rate.

Here, when the packing part 32 is used as a reference, the buffer tank 30 is connected to the liquefied gas supply line L1 at the upper position, and is connected to the boil-off gas supply line L6 at the lower position, so that the liquid phase and the gas phase can be utilized to the maximum extent. fluid nature. In addition, the buffer tank 30 may be provided on the upper side of the upper deck 104 of the bow portion 101 .

The vaporizer 40 may be provided on the regasification line L2 to regas the high-pressure liquefied gas discharged from the booster pump 21 .

Specifically, the evaporator 40 can be installed on the regasification line L2 between the first demand point 70 and the booster pump 21, so as to vaporize the high-pressure liquefied gas supplied from the booster pump 21, so that the first demand point 70 supply in the required state.

The evaporator 40 can receive the first heat medium through the heat source circulation line L3, and exchange heat between the first heat medium and the liquefied gas to vaporize the liquefied gas, and circulate the first heat medium that has exchanged heat with the liquefied gas through the heat source again. Line L3 loops.

In order to continuously supply the heat source to the first heat medium, the evaporator 40 may have a seawater heat exchanger 41 and a steam heat exchanger 62 on the heat source circulation line L3, and may additionally have a heat source pump 42 to circulate the first heat medium through the heat source. Loop on line L3.

At this time, as the first heat medium for vaporizing the liquefied gas, the vaporizer 40 can use non-explosive heat medium such as glycol water (Glycol Water), sea water (Sea Water), steam (Steam) or engine exhaust gas, and can The high-pressure vaporized liquefied gas is supplied to the place of need 70 without pressure fluctuation.

Here, the evaporator 40 can be arranged on the upper side of the upper deck 104 of the bow 101 , and the seawater heat exchanger 41 , the steam heat exchanger 62 and the heat source pump 42 can be modularized and arranged in the space inside the bow 101 .

As an example, the seawater heat exchanger 41, the steam heat exchanger 62, and the heat source pump 42 can be modularized and arranged on the side of the inside of the hull 100, preferably inside the engine room ER, but preferably arranged on the bow 101 interior space.

Hereinafter, an example in which the seawater heat exchanger 41, the steam heat exchanger 62, and the heat source pump 42 are arranged in the interior space of the bow 101 will be described as a reference, and an example in which the seawater heat exchanger 41, the steam heat exchanger 62, and the heat source pump 42 are arranged on one side or both sides of the engine room ER will be described by 5 to 9 for illustration.

The seawater heat exchanger 41 , the steam heat exchanger 62 , and the heat source pump 42 are divided up and down by at least one deck for dividing the interior space of the hull 100 up and down. As an example, in the embodiment of the present invention, the internal space of the bow part 101 is divided up and down by the first deck D1 and the second deck D2, but it is not limited thereto.

The seawater heat exchanger 41 is installed on the seawater line L4 and the heat source circulation line L3, and performs the function of exchanging heat between the seawater received through the seawater line L4 and the first heat medium received through the heat source circulation line L3, thereby to The first heat medium transfers the heat source of seawater.

The seawater heat exchanger 41 may be installed on the first deck D1 in the interior space of the bow part 101, and may be arranged at a position adjacent to the seawater outflow port H2.

As shown in FIG. 1, in the conventional gas regasification system 1, the seawater heat exchanger 41 and the heat source pump 42 are arranged on the upper side of the upper deck 104 of the hull 100, and are used to connect the seawater pump 51 and the seawater heat exchanger 41. The length of the seawater line L4 is very long. In terms of the cost of the seawater line L4, since the seawater line L4 should be corrosion-resistant and a pipe with a large diameter should be used, the cost is very high. Pretty high question.

In this way, in the embodiment of the present invention, the seawater heat exchanger 41 and the heat source pump 42 are modularized to be arranged on the first deck D1 in the interior space of the bow 101, especially on the first deck D1 connected to the seawater outlet H2. Adjacent positions can significantly reduce the sea line L4, thereby having the effect of minimizing construction costs.

In this way, in the embodiment of the present invention, the first heat medium uses a non-explosive heat medium, so that a plurality of structures (heat source supply devices) using the first heat medium can be arranged inside the hull 100, and the second heat medium can be used. Multiple structures (heat source supply devices) of one heat medium are modularized and compacted, and multiple structures (heat source supply devices) using the first heat medium can be arranged inside the hull 100 .

In addition, in the embodiment of the present invention, a seawater pump 51 arranged on the seawater line L4 may also be included.

The seawater pump 51 can supply seawater to the seawater heat exchanger 41 through the seawater line L4, and the seawater pump 51 can be arranged on the ship bottom 105 in the inner space of the bow 101 (preferably at a position adjacent to the seawater inlet H1) .

As shown in FIG. 1 , in the conventional gas regasification system 1 , the seawater pump 51 is arranged in the engine room ER, and the length of the seawater line L4 connecting the seawater pump 51 and the seawater heat exchanger 41 is very long. Therefore, as mentioned above, conventionally, the length of the seawater line L4 was very long, and there was a problem that the construction cost was considerably high.

In this way, in the embodiment of the present invention, the seawater pump 51 is arranged on the ship bottom 105 in the inner space of the bow 101, especially the seawater pump 51 is arranged at a position adjacent to the seawater inflow port H1, so that the The reduction of the seawater line L4 has the effect of being able to minimize the construction cost.

The steam heat exchanger 62 is arranged on the steam line L5 and the heat source circulation line L3, and makes the steam received through the steam line L5 and the first heat medium received through the heat source circulation line L3 perform heat exchange with each other, so as to exert additional heat transfer to the first heat source. The function of the medium to transfer the heat source of seawater. Here, the steam may exchange heat with the first heat medium after using seawater. That is, when the heat source supplied by seawater is insufficient, in order to supplement the heat source, steam can be used as a second auxiliary solution to supply the heat source to the first heat medium.

The steam heat exchanger 62 may be provided on the first deck D1 in the inner space of the bow portion 101 .

The heat source pump 42 may be provided on the heat source circulation line L3 to circulate the first heat medium through the seawater heat exchanger 41 and the steam heat exchanger 62 provided on the heat source circulation line L3.

The heat source pump 42 can be modularized with the seawater heat exchanger 41 to be arranged in the interior space of the bow 101. In addition, the heat source pump 42 is arranged on the second deck D2 in the interior space of the bow 101. The heat source pump 42 and the seawater heat exchanger 41 are divided up and down through the 1st deck D1, and are arrange|positioned.

As described above, in the embodiment of the present invention, a non-explosive heat medium is used as the first heat medium, and a plurality of structures (heat source supply devices) using the first heat medium can be modularized and arranged on the hull 100. internal. Moreover, in the embodiment of the present invention, in order to be able to arrange a plurality of structures (heat source supply devices) using the first heat medium inside the hull 100, in order to reduce the circulation flow rate of the first heat medium, there is a structure shown in FIG. System configuration and structure of multiple lines.

Next, referring to FIG. 4 , the configuration and structure of the gas regasification system will be described in detail.

FIG. 4 is a conceptual diagram showing a gas regasification system of an embodiment of the present invention.

Here, the evaporator 40 can be composed of the first heat exchanger 401 and the second heat exchanger 402 on the regasification line L2, and the seawater heat exchanger 41 can be composed of the first seawater heat exchanger 411 and the second seawater heat exchanger 411 on the heat source circulation line L3. The heat exchanger 412 is constituted, and the steam heat exchanger 62 may be constituted by the first heater 621 and the second heater 622 on the heat source circulation line L3.

At this time, the first heat exchanger 401 can use a trim heater to raise the temperature of the vaporized liquefied gas, and the second heat exchanger 402 can use an LNG vaporizer to convert the liquefied gas in the liquid phase to The function of vaporizing liquefied gas in the gas phase. In addition, the first heater 621 and the second heater 622 may be electric heaters.

In addition, in the embodiment of the present invention, it may further include a seawater parallel line L4a and a steam parallel line L5a. The seawater parallel line L4a may branch from the seawater line L4 to be connected in parallel with the second seawater heat exchanger 412. The steam parallel line L5a may be branched from the steam line L5 to be connected in parallel with the second heater 622 .

Referring to Fig. 4, the structure of the vaporizer 40 of the gas regasification system 2 of the embodiment of the present invention is analyzed in detail, the first heat exchanger 401, the first seawater heat exchanger 411, the second heat exchanger 402, and the second seawater heat exchanger 412 may be arranged sequentially on the heating source circulation line L3. Here, the first heater 621 is installed between the first seawater heat exchanger 411 and the second heat exchanger 402 on the heat source circulation line L3, and the second heater 622 is installed on the second seawater heat exchanger on the heat source circulation line L3. Between the exchanger 412 and the first heat exchanger 401 . Here, seawater may be used to heat the first heat source before steam is used.

In the embodiment of the present invention, by arranging the above-mentioned multiple structures in sequence, the flow rate of the first heat medium can be significantly reduced while maintaining the vaporization rate of the liquefied gas. A plurality of structures (heat source supply devices) of the medium are actually arranged inside the hull 100 .

In addition, the gas regasification system 2 of the embodiment of the present invention may further include a pressure maintaining device 94 .

The pressure maintaining device 94 can maintain the pressure of the first heat medium flowing on the heat source circulation line L3, and can be realized by using an inert gas.

In this way, in the embodiment of the present invention, since the pressure maintaining device 94 maintains the pressure of the first heat medium using an inert gas, there is an effect that it can be compactly arranged in the inner space of the hull 100 .

The second need place 61 receives the boil-off gas generated by the liquefied gas storage tank 10 to be used as fuel. That is, the second need point 61 requires boil-off gas, and the boil-off gas is driven as a raw material. The second place of need 61 may be a power generator (for example, DFDG), a gas combustion unit (GCU), or a boiler (for example, a boiler that generates steam), but is not limited thereto.

Specifically, the second need place 61 is connected to the boil-off gas branch line L7 to receive the boil-off gas, and the boil-off gas branch line L7 is branched from the downstream of the boil-off gas compressor 80 on the boil-off gas supply line L6. The second demand place 61 can receive the low-pressure boil-off gas pressurized by the boil-off gas compressor 80 to approximately 1 bar to 6 bar (maximum 15 bar) to be used as fuel.

In addition, the second need 61 may be a heterogeneous fuel engine that can use a heterogeneous fuel. Not only evaporated gas can be used as fuel, but oil can also be used as fuel. Gas or oil is selectively supplied. This is to stop the mixed supply of two substances having different combustion temperatures, and to prevent a reduction in the efficiency of the second demand point 61 .

Here, the second required place 61 may be provided on the deck D of the engine room ER provided inside the stern portion 103 , and the second required place 61 may be connected to the aforementioned steam heat exchanger 62 through the steam line L5 .

At this time, the steam line L5 can pass through the space inside the hull (hull) in the form of a double partition wall provided at the bottom 105 of the ship, and exchange heat with the steam at the bow 101 and the second required place 61 at the stern 103 Device 62 is connected.

The first demand place 70 can receive the liquefied gas vaporized by the vaporizer 40 for consumption. Here, the first need point 70 can receive and use the liquefied gas in the gas phase obtained by vaporizing the liquefied gas, and may be an onshore terminal installed on land or an offshore terminal installed floating on the sea.

The boil-off gas compressor 80 can pressurize the boil-off gas generated by the liquefied gas storage tank 10 to supply it to the buffer tank 30 or the second demand place 61 . Here, the boil-off gas compressor 80 may be disposed in a compressor chamber 81 , and a motor chamber 82 may be disposed on a side of the compressor chamber 81 .

Specifically, the boil-off gas compressor 80 may be installed on the boil-off gas supply line L6, and pressurize the boil-off gas generated by the liquefied gas storage tank 10 to about 6 bar to 8 bar or 6 bar to 15 bar to supply to the buffer tank 30 or It is supplied to the second demand place 61 . At this time, the second need point 61 may receive the boil-off gas through the boil-off gas branch line L7 branched from the boil-off gas supply line L6.

A plurality of boil-off gas compressors 80 may be installed to pressurize the boil-off gas in multiple stages. As an example, three boil-off gas compressors 80 may be installed to pressurize the boil-off gas in three stages. Here, as an example, the three-stage compressor is just an example, and it is not limited to three stages.

In an embodiment of the present invention, an evaporative gas cooler (not shown) may be provided at each rear end of the evaporative gas compressor 80 . When the boil-off gas is pressurized by the boil-off gas compressor 80, the temperature of the boil-off gas may rise as the pressure rises. Therefore, in this embodiment, the temperature of the boil-off gas can be lowered again by using the boil-off gas cooler. The number of evaporative gas coolers may be the same as the number of evaporative gas compressors 80 , and each evaporative gas cooler may be disposed downstream of each evaporative gas compressor 80 .

In addition, in the embodiment of the present invention, the boil-off gas compressors 80 are arranged in parallel, so that when the amount of boil-off gas generated by the liquefied gas storage tank 10 rises sharply, all of them can be accommodated, or even if the boil-off gas compressor 80 When one of them malfunctions or shuts down, the other boil-off gas compressor 80 can also be operated, so that the boil-off gas generated by the liquefied gas storage tank 10 can be efficiently accommodated and processed. Here, the boil-off gas compressor 80 may be installed on the upper side of the upper deck 104 of the bow 101 .

Thus, the ship with the gas regasification system of the present invention has the effect of maximizing the regasification efficiency of liquefied gas.

Fig. 3 is a conceptual diagram showing a gas regasification system of another embodiment of the present invention.

As shown in Figure 3, the gas regasification system 3 of other embodiments of the present invention includes a liquefied gas storage tank 10, a feed pump 20, a booster pump 21, a buffer tank 30, a vaporizer 40, a second need place 61, a first A place of need 70 , a boil-off gas compressor 80 , a boil-off gas suction unit 90 , a first pressurizing means 91 and a second pressurizing means 92 , and a nitrogen separator 93 .

Next, with reference to FIG. 3 , a gas regasification system 3 according to an embodiment of the present invention will be described.

Liquefied gas storage tank 10, feed pump 20, booster pump 21, buffer tank 30, vaporizer 40, first heat exchanger 41, second heat exchanger 42, second need place 61, first need place 70 and evaporation The structure of the gas compressor 80 is the same as or similar to that described in the gas regasification system 2 of the embodiment of the present invention.

In an embodiment of the present invention, a branching line L8 and an evaporative gas suction line L9 may be further included. A plurality of valves (not shown) whose openings can be adjusted can be provided in each line, and the supply amount of boil-off gas or liquefied gas can be controlled by adjusting the openings of each valve.

The split line L8 can be branched downstream of the vaporizer 40 on the regasification line L2 , preferably downstream of the first heat exchanger 401 , and connected to the upstream of the first demand point 70 after bypassing the boil-off gas suction unit 90 .

In the case of not driving the evaporated gas suction unit 90 , the branch line L8 can directly supply the liquefied gas re-evaporated by the vaporizer 40 to the first demand point 70 .

The boil-off gas suction line L9 connects the boil-off gas suction unit 90 and the liquefied gas storage tank 10 , and can supply the boil-off gas generated by the liquefied gas storage tank 10 to the boil-off gas suction unit 90 .

The boil-off gas suction unit 90 may be disposed downstream of the vaporizer 40 on the re-gasification line L2 to suck the boil-off gas generated by the liquefied gas storage tank 10 .

Specifically, the boil-off gas suction unit 90 can be arranged downstream of the vaporizer 40 on the re-vaporization line L2, and connected to the liquefied gas storage tank 10 through the boil-off gas suction line L9. The vaporized liquefied gas supplied from the evaporator 40 is used as the driving fluid (Driving Fluid), and the boil-off gas generated by the liquefied gas storage tank 10 is sucked through the boil-off gas suction line L9, then mixed and supplied to the first demand through the re-gasification line L2 again. At 70.

At this time, the boil-off gas suction unit 90 can receive the vaporized liquefied gas with a pressure of 50 bar to 120 bar, suck the boil-off gas from the liquefied gas storage tank 10 with a pressure of 1 bar to 1.1 bar for mixing, and the boil-off gas suction unit 90 can be Ejector, Eductor or jet pump.

The vaporized liquefied gas flowing into the boil-off gas suction unit 90 may have a pressure of 50bar to 120bar (preferably 100bar), and the boil-off gas generated by the liquefied gas storage tank 10 has a pressure of 1.00bar to 1.10bar (preferably approximately 1.06bar).

The boil-off gas suction unit 90 receives the liquefied gas re-evaporated from the vaporizer 40 as the driving fluid, and sucks the boil-off gas generated by the liquefied gas storage tank 10 for mixing. The kinetic energy is then converted into pressure again as the speed of the mixed fluid decreases at the end portion of the enlarged cross-section of the nozzle (not attached with a reference numeral) of the boil-off gas suction unit 90 .

Thus, the boil-off gas generated in the liquefied gas storage tank 10 can obtain a mixed fluid having a pressure lower than the pressure of 50 bar to 120 bar as the inflow pressure of the driving fluid. In this way, the first demand point 70 cannot be consumed with this pressure, so it is necessary to supply additional pressure to the first demand point 70 after additional pressurization means. Here, the additional pressurization means is the second pressurization described later. Pressure means 92 .

Here, since the pressure of the driving fluid is high pressure, the pressure of the suction fluid can be easily raised even with a small amount of fluid.

In this way, the gas regasification system 3 of the embodiment of the present invention processes the boil-off gas generated by the liquefied gas storage tank 10 through the boil-off gas suction device 90, so it is not necessary to construct an additional recondenser for recondensing the boil-off gas, thereby having the following As a result, the construction cost is reduced, the system becomes compact and the reliability is improved.

The first pressurizing means 91 may be provided between the boil-off gas suction unit 90 on the regasification line L2 and the vaporizer 40 , and pressurizes the vaporized liquefied gas discharged from the vaporizer 40 . In this case, the first pressurizing means 91 is means for pressurizing gas, and may be a compressor as an example.

Specifically, the first pressurizing means 91 can be arranged between the evaporative gas suction unit 90 on the revaporization line L2 and the branch point of the branch line L8, and pressurize the liquefied gas vaporized from the vaporizer 40 to above 120bar to It is supplied to the boil-off gas suction unit 90 .

That is, the first pressurizing means 91 can compensate the pressure lost in the vaporizer 40 to supply the boil-off gas suction unit 90 , and can further increase the pressure of the vaporized liquefied gas according to the intake amount of the boil-off gas generated by the liquefied gas storage tank 10 . , thus having the effect of being able to efficiently process the boil-off gas.

The second pressurizing means 92 can be arranged between the boil-off gas suction unit 90 on the revaporization line L2 and the first need place 70, and the mixed fluid (the mixture of vaporized liquefied gas and boil-off gas) discharged from the boil-off gas suction unit 90 ) for pressurization. In this case, the second pressurizing means 92 is means for pressurizing gas, and may be, for example, a compressor.

Specifically, the second pressurizing means 92 can be arranged between the connection point of the nitrogen separator 93 on the regasification line L2 and the split line L8, and pressurize the mixed fluid discharged from the boil-off gas suction unit 90 to 50 bar to 120bar, to supply to the first need 70.

That is, the second pressurizing means 92 compensates for the pressure loss in the boil-off gas suction unit 90 and supplies it to the first demand point 70 , thereby having the effect of being able to appropriately adjust the pressure required by the first demand point 70 .

The nitrogen separator 93 can be installed between the boil-off gas suction unit 90 and the second pressurization means 92 on the revaporization line L2, and the mixed fluid (mixture of vaporized liquefied gas and boil-off gas) discharged from the boil-off gas suction unit 90 can be installed The nitrogen components inside are separated and removed.

The separated nitrogen can be supplied to a nitrogen demand place (not shown) that consumes nitrogen in the ship hull 100 , and can be supplied to, for example, the pressure maintaining device 94 to maintain the pressure of the first heat medium.

In the embodiments of FIGS. 2 to 4 described above, a cargo switchboard room 1001 (Cargo SWBD room) can be arranged on the lower side of the regasification unit room 1000, and a ventilation mast V can be arranged on the upper deck 104. A cabin C and a chimney Ch are arranged on the upper upper deck 104 of the engine room ER.

Fig. 5 is a conceptual diagram of a ship with a gas regasification system according to another embodiment of the present invention, Fig. 6 is a conceptual diagram showing a gas regasification system according to another embodiment of the present invention, and Fig. 7 is a detailed illustration of the gas regasification system A conceptual diagram of a gas regasification system according to yet another embodiment of the invention. FIG. 8 is a conceptual diagram showing a glycol water circulation device according to an embodiment of the present invention.

As shown in Figures 5 to 8, the gas regasification system 4 of other embodiments of the present invention includes a liquefied gas storage tank 10, a feed pump 20, a booster pump 21, a buffer tank 30, a vaporizer 40, and a second demand point 61 , the first need place 70 and the boil-off gas compressor 80 .

In the embodiments of FIGS. 2 to 4 described above, the following technology has been described: the seawater heat exchanger 41, the steam heat exchanger 62, and the heat source pump 42 are modularized to be arranged at the bow of the inner side of the hull 100. The lower side of the upper deck 104 of the part 101, that is, the interior space of the bow part 101. Next, the invention in which the seawater heat exchanger 41 , the steam heat exchanger 62 , and the heat source pump 42 are arranged inside the engine room ER will be described with reference to FIGS. 5 to 8 .

The structures not mentioned in the structures shown in FIGS. 5 to 8 are the same as those of the vessel including the gas regasification systems 2 , 3 illustrated in FIGS. 2 to 4 . Wherein, the embodiments illustrated in FIGS. 5 to 8 differ from the ships including the gas regasification systems 2 and 3 illustrated in FIGS. 2 to 4 in the following two points.

First, in terms of the configuration of the regasification unit room 1000 for accommodating the booster pump 21, the recondenser 30, and the vaporizer 40, in the ship including the gas regasification systems 2, 3 illustrated in FIGS. 2 to 4, It is arranged on the upper deck 104 of the bow 101, but, in the gas regasification system 4 shown in FIGS. For the configuration of 2000, it will be arranged in the center of the hull, and this difference point is the first difference point (difference in the configuration position of the gas regasification system). In the ships including the gas regasification systems 2 and 3 illustrated in FIGS. 2 to 4 , intermediate heat medium supply devices such as the seawater heat exchanger 41 , the steam heat exchanger 62 , and the heat source pump 42 are disposed on the bow 101 The lower side of the upper deck 104, that is, the interior of the bow 101, but in the ship including the gas regasification system 4 shown in Figures 5 to 8, it will be arranged inside the stern 103 (preferably in the engine room ER Inside), this point of difference is the second point of difference (difference in the arrangement position of the intermediate heat medium supply device).

Hereinafter, referring to FIG. 5 to FIG. 8 , a detailed description will be given centering on the aforementioned differences.

The liquefied gas storage tank 10, the feed pump 20, the booster pump 21, the buffer tank 30, the vaporizer 40, the first heat exchanger 41, the second heat exchanger 42, the first need place 70, and the evaporated gas compressor 80 are connected with this The descriptions in the gas regasification systems 2 and 3 of the embodiment of the invention and other embodiments are the same or similar.

In an embodiment of the present invention, it may also include an ethylene glycol water storage tank 43, an expansion tank (expansion tank) 44, a regasification unit room 2000, a cargo switchboard room 2001 (Cargo SWBD room), and a transfer room TR (transfer room) , Conversion room CVT (convert room).

Here, the transport room TR and the conversion room CVT can be arranged on the third deck D4 (3rd deck), and the cargo switchboard room 2001 (Cargo SWBD room) can be arranged in the ship room C, and the ship room C can be compared with Fig. 2 to Fig. 4 Compared with the cabins arranged in the ships including the gas regasification systems 2 and 3 of the embodiment, the height is lower.

In the embodiment of the present invention, the boiler (not shown) previously installed in the engine room ER can be removed, and intermediate heat medium supply devices such as seawater heat exchanger 41, heat source pump 42, and glycol water storage tank 43 can be arranged. In front of the engine E in the engine room ER.

With the removal of the boiler, the space for the engine E to move to the stern direction on the fourth deck D5 (4th deck) is ensured, and thus it can be ensured in front of the engine E: for disposing the seawater heat exchanger 41, heat source pump 42. Space for intermediate heat medium supply devices such as glycol water storage tank 43. In this way, with the use of non-explosive heat medium, the intermediate heat medium supply device can be arranged in the ship, and can be arranged in the engine room ER in the ship, so that more space on the upper deck 104 can be ensured, so it has the advantages of making the ship The effect of increased space utilization.

At this time, the engine E may be connected via a motor (not shown) instead of being directly connected to the propeller shaft S by DFDE.

Here, four seawater heat exchangers 41 can be installed, and all of them can be arranged on the fourth deck D5 (4th deck), and the seawater pump 51 can be arranged on the board D6 (floor). In this way, the height difference between the seawater pump 51 and the seawater heat exchanger 41 is reduced, so the water head of the seawater pump 51 is reduced, thereby having the effect of reducing OPEX.

In addition, when the seawater heat exchanger 41 is arranged on the fourth deck D5 (4th deck) in the engine room ER, it may be arranged on or lower than the seawater surface. Thereby, the discharge line of the seawater discharged from the seawater heat exchanger 41 can be shortened, and a vacuum phenomenon generated when the seawater is discharged to the outside can be prevented.

In the embodiment of the present invention, the ethylene glycol water storage tank 43 is a tank for temporarily storing ethylene glycol water for the repair of the intermediate heat medium supply device (preferably the seawater heat exchanger 41), and can be arranged on the plate D6 (floor) superior.

That is, as the glycol water storage tank 43 is arranged on the lower side of the seawater heat exchanger 41, it is not necessary to construct an additional transfer pump for discharging the glycol water when repairing the intermediate heat medium supply device, thereby having The effect of reducing the construction cost.

In addition, in the embodiment of the present invention, when the heat source circulation line L3 passes through the upper deck 104 and is connected to the evaporator 40, it may be connected via the cofferdam 106 formed in front of the engine room ER.

Specifically, the heat source circulation line L3 horizontally penetrates the cofferdam 106 from the engine room ER to the cofferdam 106, enters the cofferdam 106, rises vertically in the cofferdam 106, and passes through the upper deck 104 on the cofferdam 106. To be connected with the vaporizer 40 in the regasification unit chamber 2000. At this time, a collection device (not shown) for collecting the leaked glycol water may be disposed on the lowermost side of the cofferdam 106 .

In this way, when the heat source circulation line L3 runs through the upper deck 104, it is not necessary to construct an additional ventilation system, thereby reducing construction costs.

In the embodiment of the present invention, as shown in Fig. 6 and Fig. 7, each heat source supply line L3 connected to the evaporator 40, the seawater heat exchanger 41 and the heat source pump 42 composed of four skids can constitute For a common line (commonline). At this time, as far as the carburetor 40 is concerned, the first carburetor skid block 401 to the fourth carburetor skid block 404 can be set on the first compartment 401a to the fourth car compartment 401d, and each of the first carburetor skid block 401 to the fourth carburetor Heat source supply lines L3 a to L3 d branched from the heat source supply line L3 are connected to the skid block 404 .

That is, conventionally, when the heat source supply line L3 is connected to the evaporator 40 constructed by four skid-mounted blocks, the number of penetrations of the upper deck 104 is 8 (incoming wires and outgoing wires), which reduces the durability of the upper deck 104. , but in the embodiment of the present invention, only two heat source supply lines L3 constituted as common lines are formed when penetrating the upper deck 104, thereby having the effect of improving the durability of the upper deck 104, reducing the possibility of heat source leakage, This has the effect of improving system reliability.

In this case, the heat source supply line L3 can be configured as an additional line in parallel, thereby sufficiently securing the flow rate of glycol water that can be accommodated in one heat source supply line L3. In this case, the number of lines penetrating the upper deck 104 may be four.

In the embodiment of the present invention, as shown in FIG. 8 , the intermediate heat medium supply device is arranged in the order of expansion tank 44 , seawater heat exchanger 41 , heat source pump 42 , and evaporator 40 . Conventionally, the expansion tank 44, the heat source pump 42, the seawater heat exchanger 41, and the evaporator 40 are arranged in order, but by arranging the intermediate heat medium supply device as shown in FIG. 8, the allowable pressure of the seawater heat exchanger 41 is reduced, thereby having An effect of reducing the construction cost of the seawater heat exchanger 41 .

Here, the seawater heat exchanger 41 may be a PCHE heat exchanger, the pressure of the glycol water flowing into the seawater heat exchanger 41 may be about 2.5 bar, and the glycol water flowing from the seawater heat exchanger 41 into the heat source pump 42 may be approximately 2.5 bar. The pressure of the water may be approximately 0.5 bar, and the pressure of the glycol water discharged from the heat source pump 42 may be approximately 15 bar. At this time, the pressure of the seawater flowing into the seawater heat exchanger 41 may be approximately 2bar to 3bar.

Fig. 9 is a conceptual diagram of a seawater supply device of the present invention.

As shown in FIG. 9 , the seawater supply device includes seawater tanks SC1 to SC3 and a seawater pump 51 for inflowing seawater. The seawater supply device of FIG. 9 is applicable not only to ships with the gas regasification systems 2 and 3 of FIGS. 2 to 4 , but also to ships with the gas regasification system 4 of FIGS. 5 to 8 .

In the conventional seawater supply device, the sea chest (Sea Chest) for inflowing seawater is arranged only on the lowermost side of the hull, so there is a possibility that high temperature may flow in due to the temperature of the seawater discharged from the gas revaporization system. seawater concerns.

In order to solve such a problem, in the seawater supply device of the present embodiment, the seawater tanks SC1 to SC3 are arranged on both sides of the hull at the lowermost side, and the first seawater tank SC1 (SeaChest1) and the second seawater tank SC2 (SeaChest2) are arranged on both sides of the hull. When introducing seawater, control the discharge of seawater from the left side of the hull (left discharge on the drawing), and when the third sea tank SC3 (SeaChest3) introduces seawater, control the discharge of seawater from the right side of the hull (right discharge on the drawing) , there is an effect of ensuring a constant temperature of the seawater introduced into the seawater tanks SC1 to SC3.

In addition, in the embodiment of the present invention, the sea chests SC1 and SC2 on the right side can be divided into two, the first sea chest SC1 (SeaChest1) and the second sea chest SC2 (SeaChest2). In this case, there is an effect that the temperature of the seawater flowing into the seawater tank can be further kept constant.

Above, the present invention has been described in detail through the specific embodiments, but these are only used to specifically illustrate the present invention, and the present invention is not limited thereto. Those skilled in the art can make modifications or improvements within the technical idea of the present invention.

The simple deformation or modification of the present invention belongs to the field of the present invention, and the specific protection scope of the present invention is defined by the claims.

Claims (14)

1. A vessel having a gas regasification system, characterized in that,

comprising the following steps:

a hull having an interior space, including at least one deck for dividing the interior space of the hull up and down;

a vaporizer provided on an upper outer side of the hull, the vaporizer vaporizing the liquefied gas to supply the liquefied gas to a desired place;

a heat source supply device for supplying a heat source as a non-explosive heat medium to the vaporizer so as to exchange heat with the liquefied gas in the vaporizer; and

a seawater supply device for supplying seawater to the heat source supply device so as to exchange heat with the heat source in the heat source supply device,

the heat source supply device and the seawater supply device are arranged in the inner space of the bow part of the ship body,

the heat source supply device comprises a heat source circulation line which is arranged on the cabin board and is used for circulating a heat source to the vaporizer,

the seawater supply device comprises a seawater line arranged at the lower side of the deck for moving the seawater to the heat source supply device,

One end of the seawater line is connected to a seawater inlet port formed in the bow of the hull, and the other end of the seawater line is connected to a seawater outlet port formed in the bow of the hull.

2. The vessel with a gas regasification system as claimed in claim 1, wherein,

the heat source supply device includes:

a heat source pump for supplying the heat source; and

a seawater heat exchanger for heat exchanging the heat source with seawater,

the heat source pump and the seawater heat exchanger are arranged on the heat source circulation line,

the heat source pump and the seawater heat exchanger are respectively divided and configured from top to bottom by the cabin plate.

3. A vessel with a gas regasification system as claimed in claim 2, characterized in that,

further comprises:

a seawater pump for supplying the seawater to the seawater heat exchanger,

the seawater flows in the seawater line, the seawater pump and the seawater heat exchanger are arranged on the seawater line,

the diameter of the heat source circulation line is smaller than the diameter of the seawater line.

4. A vessel with a gas regasification system as claimed in claim 3, characterized in that,

one end of the seawater line is connected with a seawater inflow port formed on the side surface of the ship body, the other end of the seawater line is connected with a seawater discharge port formed on the side surface of the ship body,

The heat source supply device is disposed in a region of the hull where the seawater discharge port is provided.

5. A vessel with a gas regasification system as claimed in claim 3, characterized in that,

the seawater pump is disposed on the bow side of the interior of the hull.

6. A vessel with a gas regasification system as claimed in claim 2, characterized in that,

also included is a steam heat exchanger for exchanging heat between the heat source and steam,

the heat source pump, the seawater heat exchanger and the steam heat exchanger are respectively divided and configured from top to bottom by the cabin plate.

7. The vessel with a gas regasification system of claim 6, wherein,

further comprises:

a boiler for generating the steam, the boiler being disposed in a nacelle of the hull,

a steam line connecting the steam heat exchanger and the boiler in such a manner as to circulate the steam;

at least a portion of the vapor line is disposed within a hull formed at a bottom of the hull.

8. The vessel with a gas regasification system as claimed in claim 7, wherein,

after utilizing the seawater, heat exchange is performed with the heat source using the steam.

9. The vessel with a gas regasification system of claim 6, wherein,

the heat source supply device is made as a module including the heat source pump, the seawater heat exchanger, or the steam heat exchanger.

10. The vessel with a gas regasification system as claimed in claim 1, wherein,

the heat source supply device is disposed on the bow side of the interior of the hull.

11. The vessel with a gas regasification system as claimed in claim 1, wherein,

the heat source supply device is disposed on the side surface of the interior of the hull.

12. The vessel with a gas regasification system as claimed in claim 11, wherein,

the heat source supply device is disposed on a side surface of a nacelle disposed inside a stern of the hull.

13. The vessel with a gas regasification system as claimed in claim 1, wherein,

the heat source is glycol water.

14. A vessel with a gas regasification system as claimed in claim 2, characterized in that,

the heat source supply device includes a pressure maintaining device that maintains a pressure of a heat source flowing in the heat source circulation line,

The pressure maintaining device maintains the pressure of the heat source using an inert gas.