KR102032424B1 - A Regasification System and Vessel having the same - Google Patents

Abstract

Regasification system according to the present invention, liquefied gas storage tank for storing the liquefied gas; A vaporizer for vaporizing the liquefied gas; And an intermediate heat medium supply device for exchanging heat with seawater to supply heat to the vaporizer, wherein the intermediate heat medium supply device includes: a circulation pump for circulating the intermediate heat medium for supplying the heat to the vaporizer; A seawater heat exchanger receiving the intermediate heat medium from the circulation pump and heating the seawater to supply the vaporizer to the vaporizer; And a shutdown valve provided upstream of the seawater heat exchanger to prevent the intermediate heat medium from moving to the seawater heat exchanger when the circulation pump is stopped.

Description

Regasification System and Vessel Having Same {A Regasification System and Vessel having the same}

The present invention relates to a regasification system and a vessel comprising the same.

In general, liquefied natural gas (Liquefied Nature Gas) is known to be a clean fuel and abundant reserves than petroleum, and its use is rapidly increasing with the development of mining and transport technology. It is common to store LNG in liquid state by reducing the temperature of methane, its main component, to below -162 at 1 atm, and the volume of liquefied methane is about 1/600 of the volume of gaseous methane in the standard state. 0.42, about one-half the share of crude oil.

LNG is liquefied for ease of transportation and vaporized at the point of use after transportation. In areas where there is a stable demand for LNG, LNG storage and regasification systems are installed on land, but in countries where demand is not constant or where there is a risk of natural disasters and terrorism, there is concern about installing LNG vaporization facilities on land.

Therefore, instead of the conventional liquefied natural gas regasification system installed on land, a vessel that supplies natural gas vaporized to the land by installing a regasification device on an LNG carrier carrying liquefied natural gas (Liquefied Natural Gas) LNG FSRU, for example, is in the spotlight.

Currently, in ships including LNG regasification apparatus, various researches and developments for efficient driving of a heat source supply device for vaporizing LNG have been conducted.

The present invention has been created to improve the prior art, the optimum re-selected fruit to be supplied to the regasification device to maximize the regasification efficiency while reducing the construction cost and regasification can maximize space utilization To provide a system and a ship comprising the same.

Regasification system according to the present invention, liquefied gas storage tank for storing the liquefied gas; A vaporizer for vaporizing the liquefied gas; And an intermediate heat medium supply device for exchanging heat with seawater to supply heat to the vaporizer, wherein the intermediate heat medium supply device includes: a circulation pump for circulating the intermediate heat medium for supplying the heat to the vaporizer; A seawater heat exchanger receiving the intermediate heat medium from the circulation pump and heating the seawater to supply the vaporizer to the vaporizer; And a shutdown valve provided upstream of the seawater heat exchanger to prevent the intermediate heat medium from moving to the seawater heat exchanger when the circulation pump is stopped.

Specifically, the apparatus may further include a suction drum satisfying the effective suction head of the circulation pump, and the suction drum may be installed at a higher position than the circulation pump.

Specifically, the seawater heat exchanger, the suction drum and the circulation pump, and includes a heat medium circulation line for circulating the intermediate heat medium, the shutdown valve is disposed between the downstream of the circulation pump and the sea water heat exchanger Can be.

Specifically, the heat medium circulation line is formed such that a height difference between the suction drum and the circulation pump is 3 m or more, and the shutdown valve is operated when the intermediate heat medium supply device is shut down to change the liquid level inside the suction drum. By preventing, the effective suction head of the circulation pump can be satisfied when the intermediate heat medium supply device is restarted.

Specifically, a shutdown first auxiliary valve provided between the circulation pump and the suction drum on the heat medium circulation line; A first line connected to said seawater heat exchanger and said circulation pump upstream on said heat medium circulation line, said first line comprising a first valve; A second line branched between the circulation pump on the heat medium circulation line and the shutdown valve and connected to the suction drum, the second line including a second valve; And a first control unit which recovers the intermediate heat medium remaining in the seawater heat exchanger to the suction drum through the first and second lines when the intermediate heat medium supply device is shut down.

Specifically, the first control unit closes the openings of the shutdown valve and the shutdown first auxiliary valve and opens the openings of the first and second valves when the intermediate heat medium supply device is shut down, thereby providing the seawater heat exchanger. The remaining intermediate heat medium may be controlled to be sucked by the first line through the circulation pump, supplied to the second line, and then supplied to the suction drum through the second line.

Specifically, a shutdown second auxiliary valve provided downstream of the sea water heat exchanger on the heat medium circulation line; A third line connecting the seawater heat exchanger and the suction drum, the third line including a third valve; A recovery pump provided between the third valve on the third line and the suction drum and supplying the intermediate heat medium remaining in the seawater heat exchanger to the suction drum; And a second controller configured to recover the intermediate heat medium remaining in the seawater heat exchanger through the third line and the recovery pump to the suction drum when the intermediate heat medium supply device is shut down.

Specifically, the second control unit closes the opening degree of the shutdown valve and the shutdown second auxiliary valve, opens the opening degree of the third valve, and operates the recovery pump when the intermediate heating medium supply device is shut down. The intermediate heat medium remaining in the seawater heat exchanger may be controlled to be sucked by the third line and supplied to the suction drum through the recovery pump.

Specifically, the intermediate heat medium is a mixed refrigerant for regasifying the liquefied gas through latent heat generated by a phase change phenomenon, and the seawater heat exchanger receives a liquid fruit from the circulation pump and completely vaporizes the gas through the seawater. After forming the intermediate heat medium of the gas is supplied to the vaporizer, the vaporizer is supplied with the intermediate heat medium of the gaseous phase from the sea water heat exchanger to heat exchange with the liquefied gas to change the intermediate heat medium of the gas phase to a complete liquid medium heat medium Can be.

Specifically, liquefied gas storage tank for storing the liquefied gas; A feeding pump for supplying the liquefied gas stored in the liquefied gas storage tank; A buffer tank for temporarily receiving the liquefied gas from the feeding pump; A boosting pump which receives the liquefied gas from the buffer tank and pressurizes the liquefied gas and supplies the pressurized gas to the vaporizer; A demand source for receiving and liquefied liquefied gas from the vaporizer; And a liquefied gas supply line connecting the liquefied gas storage tank and the demand destination and including the feeding pump, the buffer tank, the boosting pump, and the vaporizer.

Specifically, the mixed refrigerant may include R134a.

Specifically, the mixed refrigerant may be R407c or R421a.

Specifically, it may be a ship comprising the regasification system.

The regasification system and the ship including the same according to the present invention, by selecting the fruit to be supplied to the regasification system as a mixed fruit in which the phase change occurs to maximize the regasification efficiency, reduce the construction cost of the regasification apparatus and space in the ship Effective in maximizing usability.

In addition, the regasification system and the ship including the same according to the present invention, by using a mixed refrigerant capable of phase change as a heat medium for regasifying the carburetor, without supplying a separate power source to the device for supplying the mixed refrigerant to the carburetor of the mixed refrigerant It is possible to reduce construction costs and reduce power consumption by circulating only properties due to material changes.

1 is a conceptual diagram of a ship including a regasification system according to an embodiment of the present invention.
2 is a conceptual diagram of a regasification system according to an embodiment of the present invention.
3 is a graph of heat flow versus temperature of a seawater heat exchanger in a regasification system according to a conventional embodiment.
4 is a graph of heat flow versus temperature of a seawater heat exchanger in a regasification system according to an embodiment of the present invention.
5 is a layout plan view of a regasification system according to an embodiment of the present invention.
6 is a layout front view of a regasification system according to an embodiment of the present invention.
7 is a conceptual diagram of a regasification system according to another embodiment of the present invention.

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

Hereinafter, in the present specification, liquefied gas may be used to encompass all gaseous fuels which are generally stored in a liquid state, such as LNG or LPG, ethylene, ammonia, and the like. Can be expressed as This can be applied to the boil-off gas as well. In addition, LNG may be used for the purpose of encompassing not only liquid NG (Natural Gas) but also supercritical NG for convenience, and evaporation gas may be used to include not only gaseous evaporation gas but also liquefied evaporation gas. Can be.

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

1 is a conceptual diagram of a ship including a regasification system according to an embodiment of the present invention, Figure 2 is a conceptual diagram of a regasification system according to an embodiment of the present invention.

1 and 2, the vessel 1 including the regasification system 2 according to an embodiment of the present invention, the liquefied gas storage tank 10, the feeding pump 20, the buffer tank ( 30, the boosting pump 40, the vaporizer 50, the intermediate heat medium supply device 60 and the demand destination 70, the vessel 1, the regasification system 2 is installed, the bow portion 101, the central portion It has a hull (not shown) comprised of the 102, the stern part 103, the upper deck 104, and the ship bottom part 105. As shown in FIG.

The ship 1 including the regasification system 2 according to the embodiment of the present invention, the propeller shaft (S) produced power from the propulsion engine E of the engine room ER disposed in the stern part 103. Propulsion by propagating to propeller P, and regasification system 2 can be arranged on upper deck 104 of bow 101 of vessel 1, but the arrangement position is not limited thereto. Do not.

In addition, the vessel 1 recovers the liquefied gas provided with a regasification system 2 in the liquefied gas carrier ship (ship) 1 in order to regasify the liquefied gas at sea to supply the liquefied gas to the land terminal. It may be a LNG vessel (LNG RV) or a floating liquefied gas storage and regasification plant (FSRU).

Hereinafter, a ship 1 including a regasification system 2 according to an embodiment of the present invention will be described with reference to FIGS. 1 and 2.

Prior to describing a vessel 1 including a regasification system 2 according to an embodiment of the present invention, each of the components of the regasification system 2 disposed on the vessel 1 and its individual components are organic. A description will be given of the basic flow path connected to. Here, the flow path may be a line through which the fluid flows, but is not limited thereto, and any flow path may be used.

In the embodiment of the present invention, the liquefied gas supply line (L1) is included. Here, each of the lines may be provided with valves (not shown) that can adjust the opening degree, and the supply amount of the boil-off gas or liquefied gas may be controlled by adjusting the opening degree of each valve.

The liquefied gas supply line L1 connects the liquefied gas storage tank 10 and the demand destination 70 and includes a feeding pump 20, a buffer tank 30, a boosting pump 40, and a vaporizer 50. The liquefied gas stored in the liquefied gas storage tank 10 is supplied to the buffer tank 30 through the feeding pump 20 and then supplied to the boosting pump 40, and compressed by the high pressure in the boosting pump 40 to the vaporizer 50. ) And then vaporized to supply to the demand destination (70).

Hereinafter, individual configurations that are organically formed by the above-described line L1 to implement the regasification system 2 will be described.

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

Here, the liquefied gas storage tank 10 may be disposed inside the hull and may be formed as four, for example, in front of the engine room ER. In addition, the liquefied gas storage tank 10 is, for example, a membrane type tank, but not limited thereto, and various types such as a stand-alone tank are not particularly limited.

In the liquefied gas storage tank 10, a cofferdam (not shown) may be disposed between each liquefied gas storage tank 10, and a cofferdam between the engine room ER and the liquefied gas storage tank 10. This can be arranged.

The feeding pump 20 is provided on the liquefied gas supply line L1 and installed inside or outside the liquefied gas storage tank 10 to store the liquefied gas stored in the liquefied gas storage tank 10 in the buffer tank 30. Can be supplied as

Specifically, the feeding pump 20 is provided between the liquefied gas storage tank 10 and the buffer tank 30 on the liquefied gas supply line (L1) to primary liquefied gas stored in the liquefied gas storage tank 10 It may be pressurized and supplied to the buffer tank 30.

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

In this case, the feeding pump 20 may be a latent pump when provided inside the liquefied gas storage tank 10, and stored in the liquefied gas storage tank 10 when the feeding pump 20 is installed outside the liquefied gas storage tank 10. It may be provided at a position inside the hull lower than the level of the liquefied gas and may be a centrifugal pump.

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

Specifically, the buffer tank 30 may be supplied with the liquefied gas stored in the liquefied gas storage tank 10 from the feeding pump 20 through the liquefied gas supply line (L1), by temporarily storing the supplied liquefied gas The liquefied gas may be separated into a liquid phase and a gaseous phase, and the separated liquid phase may be supplied to the boosting pump 40.

That is, the buffer tank 30 temporarily stores the liquefied gas to separate the liquid phase and the gaseous phase, and supplies the complete liquid phase to the boosting pump 40 so that the boosting pump 40 has a net positive suction head (NPSH). ), Thereby preventing the cavitation (Cavitation) in the boosting pump (40).

In addition, the buffer tank 30 may be connected to the boil-off gas supply line (not shown) to receive the boil-off gas generated from the liquefied gas storage tank 10 and temporarily store the boil-off gas.

Specifically, the buffer tank 30 may be temporarily stored by receiving the boil-off gas generated in the liquefied gas storage tank 10 from the boil-off gas compressor (not shown) through the boil-off gas supply line.

Through this, the buffer tank 30 may be recondensed by liquefying the temporarily stored liquefied gas supplied from the liquefied gas supply line L1 and the temporarily stored evaporated gas received from the evaporated gas supply line. Here, the buffer tank 30 may be formed in a pressure vessel type capable of withstanding pressure, and may endure 6 to 8 bar or 6 to 15 bar.

Therefore, the buffer tank 30 is supplied with the boil-off gas and the liquefied gas through a boil-off gas compressor and a feeding pump 20 at a pressure of about 6 to 8 bar (or 6 to 15 bar), and the low-pressure boil-off gas or the liquefied gas. The recondensation efficiency is more improved, and recondensing in the state of maintaining the pressure is supplied to the boosting pump 40 to lower the compression load of the boosting pump 40.

Boosting pump 40 may be provided between the buffer tank 30 and the vaporizer 50 on the liquefied gas supply line (L1), from the liquefied gas or buffer tank 30 supplied from the feeding pump 20 The supplied liquefied gas may be pressurized to 50 to 120 bar and supplied to the vaporizer 50.

The boosting pump 40 may pressurize the liquefied gas according to the pressure required by the customer 70, and may be configured as a centrifugal pump.

The vaporizer 50 may be provided on the liquefied gas supply line L1 to re-gas the liquefied gas of the high pressure discharged from the boosting pump 40.

Specifically, the vaporizer 50 is provided on the liquefied gas supply line L1 between the demand destination 70 and the boosting pump 40, and vaporizes the high pressure liquefied gas supplied from the boosting pump 40 to demand demand 70. Can be supplied in the desired state.

The vaporizer 50 receives the intermediate heat medium through the intermediate heat medium supply device 60 and heat-exchanges with the liquefied gas to vaporize the liquefied gas.

The vaporizer 50 may use a mixed refrigerant in which a phase change exists as an intermediate heat medium for vaporizing the liquefied gas, and supply the high-pressure vaporized liquefied gas to the demand destination 70 without a pressure change. At this time, the vaporizer 50 may receive the completely vaporized mixed refrigerant from the seawater heat exchanger 62 to heat-exchange with the liquefied gas to vaporize the liquefied gas.

The vaporizer 50 may be provided singly without providing a separate trim heater on the liquefied gas supply line (L1).

That is, in the present invention, by using a mixed refrigerant phase-changeable as an intermediate heat medium for supplying heat to the vaporizer 50, further regasification of the temperature suitable for the demand destination 70 without additional construction of a device for supplying heat to the liquefied gas Since the liquefied gas can be supplied, the liquefied gas may be provided on the liquefied gas supply line L1 without being provided with a separate trim heater.

The intermediate heat medium supply device 60 uses a mixed refrigerant that is phase-changed during heat exchange with heat exchange with seawater to supply heat to the vaporizer 50.

The mixed refrigerant is a substance in which a phase change occurs during heat exchange with seawater, and the evaporation temperature curve may have a positive slope, and after the heat exchange with seawater, the liquefied gas may be separated from the vaporizer 50 without additional heat exchange. Can be heat exchanged. Where the evaporation temperature curve is the curve on the temperature-mass flow chart.

In this case, the mixed refrigerant may be phase-changed from the liquid phase to the gas phase by heat exchange with seawater, and may be phase-changed from the gas phase to the liquid phase upon heat exchange with liquefied gas.

The mixed refrigerant is heat-exchanged with seawater in a seawater heat exchanger (62), and is phase-changed from a liquid phase to a complete gaseous phase and supplied to the vaporizer (50). Can be supplied to the suction drum 63.

The mixed refrigerant is a refrigerant including an R134a series, preferably R407c, and most preferably R421a.

Specifically, it will be described with reference to FIGS. 3 and 4.

3 is a graph of heat flux versus temperature of a seawater heat exchanger in a regasification system according to a conventional embodiment, and FIG. 4 is a graph of heat flux versus temperature of a seawater heat exchanger in a regasification system according to an embodiment of the present invention. It is a graph.

3 and 4 will be described below with respect to the phase change of the mixed refrigerant generated in the seawater heat exchanger 62 of the present invention.

3 is a graph of heat flow versus temperature in a seawater heat exchanger when a single refrigerant is used instead of a mixed refrigerant, wherein C1 is a heat diagram by seawater and C2 is a heat diagram of a single refrigerant.

Looking at C2, in the case of a single refrigerant there is no change in temperature if the pressure is constant during the phase change process. Accordingly, since the phase change temperature is lowered as the pressure decreases, the pressure loss of the single refrigerant naturally occurs in the seawater heat exchanger, so that the temperature of the single refrigerant is lowered during the phase change process of the single refrigerant. (A to B in Fig. 3; evaporation temperature curve)

Therefore, as shown by C2 in FIG. 3, when the first inflow into the seawater heat exchanger, the temperature of a single refrigerant rises, and then the temperature drops from the point A indicated by X1, which is a phase change section (from point A to point B), and then again. At point B, the temperature rises.

It can be seen that the logarithm difference temperature (LMDT) and minimum approach temperature are very narrow because the temperature difference between C1 and C2 is small at the X1 point, which leads to an increase in the size of the heat exchanger and an increase in purchase cost.

In order to solve this problem, the present invention solves this problem by using a mixed refrigerant and using a refrigerant including the R134a series (preferably R407c, most preferably R421a) among the mixed refrigerants.

4 is a graph of heat flow versus temperature in a seawater heat exchanger when a mixed refrigerant is used instead of a single refrigerant, wherein C1 is a heat diagram by seawater and C3 is a heat diagram of the mixed refrigerant.

Looking at C3, the temperature of the mixed refrigerant is increased even if the pressure is kept constant during the phase change process. This is especially true for refrigerants containing the R134a family. Accordingly, since the phase change temperature rises even if the pressure decreases, the temperature of the mixed refrigerant rises during the phase change process of the mixed refrigerant even if a pressure loss of the mixed refrigerant occurs naturally in the seawater heat exchanger.

Therefore, the temperature of the mixed refrigerant rises at the first inflow into the seawater heat exchanger as shown by C3 in FIG. 4, and the temperature rises at the point A 'indicated by the phase change section (evaporation temperature curve) X2 and also at the point B'. It has a curve in which the temperature continues to rise.

Due to this, the seawater heat exchanger 62 of the present invention can increase the LMDT and the minimum approach temperature in the heat exchanger, which can increase the heat exchange efficiency to reduce the size of the heat exchanger and reduce the construction cost. Bring.

The intermediate heat medium supply device 60 includes a circulation pump 61, a seawater heat exchanger 62, a suction drum 63, a heat medium circulation line 64, a pressure compensation line 65, and a minimum flow rate circulation line 66. It may include.

The circulation pump 61 is disposed between the suction drum 63 and the seawater heat exchanger 62 on the heat medium circulation line 64, so that the intermediate heat medium, that is, the mixed refrigerant, can be circulated on the heat medium circulation line 64. Thereby supplying the mixed refrigerant to the vaporizer 50.

The circulation pump 61 may be driven such that a pressure margin capable of pressurizing the mixed refrigerant is higher than a pressure margin when the evaporation temperature curve of the mixed refrigerant has a negative slope. The pressure margin here may be, for example, 2 to 4.5 bar. Through this, there is an effect to maximize the heat exchange efficiency of the mixed refrigerant in the sea water heat exchanger 62 and the vaporizer (50).

The circulation pump 61 is formed so as not to be immersed in the liquefied gas, and may be formed to receive the liquefied gas from which the suction head 63 satisfies the effective suction head. In this case, the circulation pump 61 may be formed in a centrifugal type or a reciprocating type.

That is, the circulation pump 61 is formed to receive the liquefied gas satisfying the effective suction head from the suction drum 63, thereby preventing the occurrence of cavitation, and may not be constituted by a latent pump and may use a general pump. This reduces the cost of construction and maximizes safety.

The seawater heat exchanger 62 is disposed between the circulation pump 61 and the seawater heat exchanger 62 on the heat medium circulation line 64, and receives liquid mixed refrigerant from the circulation pump 61 and mixes the seawater through the seawater. The refrigerant can be completely vaporized from the liquid phase to the complete gas phase.

The suction drum 63 is disposed between the vaporizer 50 and the circulation pump 61 on the heat medium circulation line 64, and after temporarily storing the completely mixed liquid refrigerant supplied from the vaporizer 50, the circulation pump ( 61).

In addition, the suction drum 63 may be formed to satisfy the effective suction head of the circulation pump 61.

The suction drum 63 may be installed at a position higher than the circulation pump 61 to satisfy the effective suction head of the circulation pump 61 during the initial operation of the circulation pump 61. That is, the suction drum 63 may be formed to have a height difference of 3 m or more from the circulation pump 61 and may be connected to the circulation pump 61 through the heat medium circulation line 64.

At this time, the suction drum 63, the pressure compensation line 65 in order to additionally satisfy the effective suction head of the circulation pump 61 during the medium-term operation of the circulation pump 61, that is, after the initial operation and before the end of the operation. Through the compensation of the internal pressure through the effective suction head of the circulation pump 61 can be satisfied.

Through this, the safe driving is possible with the circulation pump 61 and the durability is improved, so that the driving reliability of the intermediate heat medium supply device 60 is improved.

The heat medium circulation line 64 is constructed in the order of the vaporizer 50, the suction drum 63, the circulation pump 61, the seawater heat exchanger 62, and the mixed refrigerant in the vaporizer 50, the suction drum 63, The circulation pump 61 may be circulated in order of the seawater heat exchanger 62.

At this time, the heat medium circulation line 64, when connecting the vaporizer 50 and the suction drum 63, may be connected to the lower side of the suction drum (63).

The pressure compensation line 65 is branched on the heat medium circulation line 64 to compensate for the internal pressure of the suction drum 63.

Specifically, the pressure compensation line 65 is branched between a section in which the intermediate heat medium (mixed refrigerant) in the gas phase on the heat medium circulation line 64 flows, that is, downstream of the seawater heat exchanger 62 and upstream of the vaporizer 50. The internal pressure of the suction drum 63 may be compensated by being connected to the suction drum 63 and supplying the intermediate heat medium in the gas phase to the suction drum 63.

The pressure compensation line 65 increases the internal pressure of the suction drum 63 during the normal operation of the intermediate heat medium supply device 60, and internally the suction drum 63 when the intermediate heat medium supply device 60 stops. Can reduce the pressure. In this case, the gas exiting from the suction drum 63 through the pressure compensation line 65 may be introduced into the vaporizer 50 and liquefied.

In the present invention for this control, a separate control unit (not shown) may be additionally provided, and the pressure compensation line 65 may further include a return valve 651 and a supply means 652.

The controller may control the pressure compensation line 65 to prevent the internal pressure of the suction drum 63 from rising when the intermediate heat medium supply device 60 is stopped.

That is, the controller may control the gas inside the suction drum 63 to cool down when the intermediate heat medium supply device 60 stops and the internal pressure of the suction drum 63 rises.

Specifically, when the pressure in the suction drum 63 rises when the intermediate heat medium supply device 60 stops, the control unit opens the opening degree of the return valve 651 and operates the supply means 652 to operate the suction drum. The suction drum (63) is supplied to the vaporizer (50) through the pressure compensation line (65), and the liquefied gas flows to the vaporizer (50), the suction drum supplied through the pressure compensation line (65) 63) After allowing the gas inside to cool, it may be controlled to return to the suction drum 63 again.

Through this, the internal pressure of the suction drum 63 for temporarily storing the mixed refrigerant in which the phase change occurs can be efficiently adjusted, thereby improving driving reliability of the intermediate heat medium supply device 60, and increasing the internal pressure of the suction drum 63. By using the pressure compensation line 65 and the carburetor 50 without establishing a separate control device for adjusting, there is an effect that the construction cost is reduced.

The minimum flow rate circulation line 66 is branched downstream of the circulation pump 61 on the heat medium circulation line 64 to be connected to the suction drum 63 to secure the minimum flow rate of the intermediate heat medium flowing into the circulation pump 61. It is possible to circulate the intermediate heat medium between the suction drum 63 and the circulation pump 61 so as to be. Here, the minimum flow rate circulation line 66 may also be referred to as a second line and may include a second valve 661.

In the present invention, the shutdown valve 81, the shutdown first auxiliary valve 811, the first line 82, the first valve 821 so as to satisfy the effective suction head even when the circulation pump 61 is restarted after stopping. ), A third line 83, a third valve 831, a recovery pump 832, a shutdown second auxiliary valve 84, and first and second controllers (not shown).

The shutdown valve 81 is provided on the heat medium circulation line 64 upstream of the sea water heat exchanger 62 to prevent the intermediate heat medium from moving to the sea water heat exchanger 62 when the circulation pump 61 is stopped. do.

The shutdown valve 81 is arranged between the downstream of the circulation pump 61 on the heat medium circulation line 64 and the upstream of the seawater heat exchanger 62, and is operated when the intermediate heat medium supply device 60 is shut down to operate the suction drum 63. By preventing the internal liquid level fluctuation, the effective suction head of the circulation pump 61 can be sufficiently satisfied through the suction drum 63 when the intermediate heat medium supply device 60 is restarted.

The shutdown first auxiliary valve 811 is provided between the circulation pump 61 on the heat medium circulation line 64 and the suction drum 63, and is connected to the first controller in a wired or wireless manner to open and close the opening.

The first line 82 is connected upstream of the circulation pump 61 on the seawater heat exchanger 62 and the heat medium circulation line 64, and may include a first valve 821.

The first valve 821 may be disposed on the first line 82 to be connected to the first controller in a wired or wireless manner so that the opening degree may be opened or closed.

The second line 66 may be branched between the circulation pump 61 on the heat medium circulation line 64 and the shutdown valve 81 to be connected to the suction drum 63, and further include a second valve 661. Can be.

The second valve 661 may be disposed on the second line 66 to be connected to the first controller in a wired or wireless manner to open and close the opening degree.

The third line 83 connects the seawater heat exchanger 62 and the suction drum 63, and may further include a third valve 831 and a recovery pump 832.

The third valve 831 is disposed closer to the seawater heat exchanger 62 than the recovery pump 832 on the third line 83, and may be connected to the second control unit by wire or wirelessly to open and close the opening.

The recovery pump 832 is disposed closer to the suction drum 63 than the third valve 831 on the third line 83, and the intermediate heat medium remaining in the seawater heat exchanger 62 is transferred to the suction drum 63. Can supply

The recovery pump 832 may be connected to the second control unit by wire or wirelessly to open and close the opening degree.

The shutdown second auxiliary valve 84 is provided downstream of the seawater heat exchanger 62 on the heat medium circulation line 64, and may be connected to the second control unit by wire or wirelessly to open and close the opening.

The first control unit controls the suction drum 63 to recover the intermediate heat medium remaining in the seawater heat exchanger 62 through the first and second lines 82 and 66 when the intermediate heat medium supply device 60 is shut down. can do.

Specifically, the first control unit closes the opening degree of the shutdown valve 81 and the shutdown first auxiliary valve 811 when the intermediate heating medium supply device 60 shuts down, and the opening degrees of the first and second valves 821 and 661. After opening, the intermediate heat medium remaining in the seawater heat exchanger 62 is sucked by the first line 82 through the circulation pump 61 and supplied to the second line 66, and then the second line 66 is opened. It may be controlled to be supplied to the suction drum 63 through.

The second control unit may recover the intermediate heat medium remaining in the seawater heat exchanger 62 through the third line 83 and the recovery pump 832 to the suction drum 63 when the intermediate heat medium supply device 60 is shut down. have.

Specifically, when the intermediate heating medium supply device 60 is shut down, the second control unit closes the opening degree of the shutdown valve 81 and the shutdown second auxiliary valve 84 and opens and recovers the opening degree of the third valve 831. The pump 832 may be operated to control the intermediate heat medium remaining in the seawater heat exchanger 62 to be sucked by the third line 83 through the recovery pump 832 and supplied to the suction drum 63.

As a result, in the present invention, stable circulation of the intermediate heat medium is possible even when the intermediate heat medium supply device 60 is restarted, thereby improving driving reliability.

The demand destination 70 can receive and consume the liquefied gas regasified by the vaporization price 50.

Since the vaporizer 50 is provided on the liquefied gas supply line L1 in the present invention, the demand destination 70 receives the liquefied liquefied gas through the vaporizer 50 without additional heating other than the vaporizer 50 and consumes it. can do.

Here, the demand destination 70 may vaporize the liquefied gas and receive and use the liquefied gas in a gaseous state, and may be a land terminal installed on the land or a sea terminal installed floating on the sea.

Hereinafter, the arrangement of the components of the regasification system 2 will be described with reference to FIGS. 5 and 6.

5 is a layout plan view of a regasification system according to an embodiment of the present invention, and FIG. 6 is a layout front view of a regasification system according to an embodiment of the present invention.

In the present invention, a plurality of boosting pumps 40 are provided to be connected to one buffer tank 30, and may be disposed radially about one buffer tank 30.

In addition, in the present invention, a plurality of vaporizers 50 may be provided, and may be disposed on the plurality of boosting pumps 40, and may be formed of a printed circuit board type heat exchanger (PCHE).

In addition, in the present invention, a plurality of intermediate heat medium supply devices 60 may be provided, and may be disposed radially around one buffer tank 30.

In the intermediate heat medium supply device 60, the seawater heat exchanger 62, the circulation pump 61, and the suction drum 63 may be disposed radially with respect to one buffer tank 30.

Here, the plurality of boosting pumps 40 and the circulation pump 61 and one buffer tank 30 of the intermediate heat medium supply device 60 may all be disposed on the upper deck 104, and the vaporizer 50 and the intermediate The seawater heat exchanger 62 and the suction drum 63 of the heat medium supply device 60 are stacked on the boosting pump 40 and the circulation pump 61, and are disposed on the first deck D, and the buffer tank ( It may be formed to be disposed in a lower position than 30).

Here, the suction drum 30 and the circulation pump 61 may be arranged such that the height difference is about 3 m or more.

Due to the arrangement of the above configuration it can be properly disposed on the upper deck 104 of the vessel 1 has the effect of maximizing space utilization.

As described above, the regasification system 2 and the vessel 1 including the same according to the present invention select the fruit supplied to the regasification system 2 as a mixed fruit in which a phase change occurs, thereby maximizing regasification efficiency and recovering. It is effective in reducing the construction cost of the fire engine and maximizing the space utilization in the ship (1).

Hereinafter, the regasification system 2 according to another embodiment of the present invention will be described with reference to FIG. 7.

7 is a conceptual diagram of a regasification system according to another embodiment of the present invention.

As shown in FIG. 7, the vessel 1 including the regasification system 2 according to another embodiment of the present invention includes a liquefied gas storage tank 10, a feeding pump 20, and a buffer tank 30. , Boosting pump 40, vaporizer 50, intermediate heat medium supply device 60a, and demand source 70.

In this embodiment, the configuration except for the intermediate heat medium supply device 60a is the same as or similar to those in the previous embodiment, so that the configuration is replaced with the same reference numerals for convenience of each configuration, but necessarily refer to the same configuration. It is not.

Hereinafter, a vessel 1 including a regasification system 2 according to another embodiment of the present invention will be described with reference to FIG. 7, and the intermediate heat medium supply device 60a will be described in detail.

The intermediate heat medium supply device 60a has a mixed refrigerant for supplying latent heat to the vaporizer 50 through a phase change phenomenon, and arranges an upper region for operating the mixed refrigerant in the gas phase rather than a region for operating the mixed refrigerant in the liquid phase. The thermosiphon effect of the mixed refrigerant allows the mixed refrigerant to circulate without a separate power source.

That is, in the present invention, the intermediate heat medium supply device 60a is not provided with a power device for circulating the intermediate heat medium, such as a pump or a compressor, and therefore, a configuration such as a suction drum is not provided separately, and the seawater heat exchanger 62a is provided. It may include a heat medium circulation line 64a and a flow control valve 67.

The seawater heat exchanger 62a may be disposed on the heat medium circulation line 64a to completely vaporize the mixed refrigerant by heat-exchanging the intermediate heat medium, that is, the mixed refrigerant and the seawater, and may be disposed below the vaporizer 50.

The seawater heat exchanger 62a may be disposed below the upper deck 104, i.e., under the upper deck 104, and may be disposed such that the height difference from the vaporizer 50 is 15 to 25 m. In this case, the vaporizer 50 may be disposed above the upper deck 104.

As a result, the intermediate heat medium that becomes liquid in the vaporizer 50 accumulates water head pressure (density * gravity acceleration * material (fluid) height) up to the seawater heat exchanger 62a by gravity and high density. ), The intermediate heat medium descends to the seawater heat exchanger 62a, and the intermediate heat medium that becomes the gaseous phase in the seawater heat exchanger 62a generates a rising force due to the characteristics of the gas having a low density, thereby causing You will rise. At this time, since the gas has a low density, since the pressure loss due to the heat medium circulation line 64a itself is less, the rise from the seawater heat exchanger 62a to the vaporizer 50 is sufficiently possible.

Therefore, the heat medium circulation line 64a is provided with a seawater heat exchanger 62a, a vaporizer 50, and a flow control valve 67, and performs flow control through the control of the flow control valve 67, and a separate power source. Only through the rise and fall due to the material properties of the intermediate heat medium, ie the mixed refrigerant.

As described above, the regasification system 2 according to the present invention and the vessel 1 including the same supply the mixed refrigerant to the vaporizer 50 by using a mixed refrigerant capable of phase change to a heat medium for regasifying the vaporizer 50. By circulating only the properties according to the material change of the mixed refrigerant without installing a separate power source, the construction cost is reduced and power consumption is significantly reduced by nearly 50%.

Although the present invention has been described in detail through specific examples, it is intended to describe the present invention in detail, and the present invention is not limited thereto, and should be understood by those skilled in the art within the technical spirit of the present invention. It is obvious that the modifications and improvements are possible.

All simple modifications and variations of the present invention fall within the scope of the present invention, and the specific scope of protection of the present invention will be apparent from the appended claims.

1: ship 2: regasification system
10: liquefied gas storage tank 20: feeding pump
30: buffer tank 40: boosting pump
50: carburetor 60,60a: intermediate heat medium feeder
61: circulating pump 62,62a: seawater heat exchanger
63: suction drum 64, 64a: heating medium circulation line
65: pressure compensation line 651: return valve
652: supply means 66: second line (minimum flow rate circulation line)
661: 2nd valve 67: flow control valve
70: customer 81: shutdown valve
811: shutdown first auxiliary valve 82: first line
821: first valve 83: third line
831: third valve 832: recovery pump
84: shutdown second auxiliary valve 101: bow portion
102: center portion 103: stern portion
104: upper deck 105: bottom
ER: Engine Room E: Engine
S: Propeller Shaft P: Propeller
D: First deck L1: Liquefied gas supply line

Claims (13)

Liquefied gas storage tank for storing the liquefied gas;
A vaporizer for vaporizing the liquefied gas; And
An intermediate heat medium supply device for heat exchange with sea water to supply heat to the vaporizer,
The intermediate heat medium supply device,
A circulation pump circulating an intermediate heating medium for supplying the heat to the vaporizer;
A seawater heat exchanger receiving the intermediate heat medium from the circulation pump and heating the seawater to supply the vaporizer to the vaporizer; And
And a shutdown valve provided upstream of said seawater heat exchanger to prevent said intermediate heat medium from moving to said seawater heat exchanger when said circulation pump is stopped. The method of claim 1,
Further comprising a suction drum to satisfy the effective suction head of the circulation pump,
The suction drum,
Regasification system, characterized in that installed in a higher position than the circulation pump. The method of claim 2,
It includes the seawater heat exchanger, the suction drum and the circulation pump, and comprises a heat medium circulation line for circulating the intermediate heat medium,
The shutdown valve
And a regasification system disposed downstream of the circulation pump and between the seawater heat exchanger. The method of claim 3, wherein
The heat medium circulation line is formed such that a height difference between the suction drum and the circulation pump is 3 m or more,
The shutdown valve is operated when the intermediate heat medium supply device is shut down to prevent the liquid level fluctuation inside the suction drum, so that the effective suction head of the circulation pump is satisfied when the intermediate heat medium supply device is restarted. Regasification system. The method of claim 4, wherein
A shutdown first auxiliary valve provided between the circulation pump on the heat medium circulation line and the suction drum;
A first line connected to said seawater heat exchanger and said circulation pump upstream on said heat medium circulation line, said first line comprising a first valve;
A second line branched between the circulation pump on the heat medium circulation line and the shutdown valve and connected to the suction drum, the second line including a second valve; And
And a first control unit for recovering the intermediate heat medium remaining in the seawater heat exchanger to the suction drum through the first and second lines when the intermediate heat medium supply device is shut down. The method of claim 5, wherein the first control unit,
Upon shutting down the intermediate heat supply device, by closing the opening degree of the shutdown valve and the shutdown first auxiliary valve and opening the opening degree of the first and second valves,
The intermediate heat medium remaining in the sea water heat exchanger is sucked by the first line through the circulation pump and supplied to the second line, and then controlled to be supplied to the suction drum through the second line. System. The method of claim 4, wherein
A shutdown second auxiliary valve provided downstream of the seawater heat exchanger on the heat medium circulation line;
A third line connecting the seawater heat exchanger and the suction drum, the third line including a third valve;
A recovery pump provided between the third valve on the third line and the suction drum and supplying the intermediate heat medium remaining in the seawater heat exchanger to the suction drum; And
And a second control unit for recovering the intermediate heat medium remaining in the seawater heat exchanger to the suction drum through the third line and the recovery pump when the intermediate heat medium supply device is shut down. The method of claim 7, wherein the second control unit,
Upon shutdown of the intermediate heat supply device, closing the opening degree of the shutdown valve and the shutdown second auxiliary valve, opening the opening degree of the third valve, and operating the recovery pump,
And the intermediate heat medium remaining in the seawater heat exchanger is controlled to be sucked by the third line through the recovery pump and supplied to the suction drum. The method of claim 4, wherein
The intermediate heat medium is a mixed refrigerant for regasifying the liquefied gas through latent heat generated by a phase change phenomenon,
The sea water heat exchanger,
Receiving liquid fruit from the circulation pump to completely vaporize through the sea water to form an intermediate heat medium of the gaseous phase and then supply to the vaporizer,
The carburetor,
And receiving the intermediate heat medium of the gaseous phase from the seawater heat exchanger to heat exchange with the liquefied gas to change the intermediate heat medium of the gas phase into a complete liquid medium heat medium. The method of claim 9,
Liquefied gas storage tank for storing the liquefied gas;
A feeding pump for supplying the liquefied gas stored in the liquefied gas storage tank;
A buffer tank for temporarily receiving the liquefied gas from the feeding pump;
A boosting pump which receives the liquefied gas from the buffer tank and pressurizes the liquefied gas and supplies the pressurized gas to the vaporizer;
A demand source for receiving and liquefied liquefied gas from the vaporizer; And
And a liquefied gas supply line connecting said liquefied gas storage tank and said demand destination, said liquefied gas supply line including said feeding pump, said buffer tank, said boosting pump and said vaporizer. The method of claim 9, wherein the mixed refrigerant,
A regasification system comprising R134a. The method of claim 11, wherein the mixed refrigerant,
Regasification system, characterized in that R407c or R421a. 13. A ship comprising the regasification system of any of claims 1-12.

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