KR101947232B1 - A Regasification System Of Gas and Vessel having same - Google Patents

Abstract

A ship equipped with a gas regeneration system according to the present invention comprises a pump unit for pressurizing liquefied gas stored in a liquefied gas storage tank; A vaporizer for vaporizing the liquefied gas and supplying it to a customer; And a heat exchange unit for exchanging heat between the evaporated gas generated in the liquefied gas storage tank and the liquefied gas supplied from the pump, wherein the vaporization unit and the heat exchange unit are formed as one module.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a gas regeneration system,

The present invention relates to a gas regeneration system and a vessel including the same.

Generally, it is known that LNG is a clean fuel and its reserves are more abundant than petroleum, and its usage is rapidly increasing as mining and transfer technology develops. This LNG is generally stored in a liquid state at a temperature of -162 ° C. or less under 1 atm of the main component. The volume of liquefied methane is about 1/600 of the volume of methane in a gaseous state in a standard state, Is 0.42, which is about one half of the specific gravity of crude oil.

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

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

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

The present invention has been made to improve the prior art, and it is an object of the present invention to provide a gas regeneration system capable of maximizing the regeneration efficiency of liquefied gas and a vessel including the same.

A gas regeneration system according to the present invention comprises: a pump section for pressurizing liquefied gas stored in a liquefied gas storage tank; A vaporizer for vaporizing the liquefied gas and supplying it to a customer; And a heat exchange unit for exchanging heat between the evaporated gas generated in the liquefied gas storage tank and the liquefied gas supplied from the pump, wherein the vaporization unit and the heat exchange unit are formed as one module.

Specifically, it is preferable that the evaporative gas compressor further comprises: an evaporative gas compressor which pressurizes the evaporative gas generated in the liquefied gas storage tank and supplies the pressurized gas to a power generation engine, wherein the evaporative gas compressor includes at least a part of the evaporative gas supplied to the power generation engine, Can supply.

Specifically, the pump unit may include: a first pump that supplies the liquefied gas stored in the liquefied gas storage tank to the customer; And a second pump that receives the liquefied gas from the first pump and pressurizes the liquefied gas to a high pressure.

Specifically, the apparatus further includes a temporary storage tank provided between the first pump and the second pump, and the evaporated gas and the liquefied gas heat-exchanged in the heat exchange unit may be supplied to the temporary storage tank.

The controller may further include a controller for controlling the evaporation gas supplied to the heat exchanger according to an amount of the evaporation gas generated in the liquefied gas storage tank.

Specifically, the apparatus further includes an evaporative gas compressor that pressurizes the evaporative gas generated in the liquefied gas storage tank to supply it to the power generation engine or supplies the evaporated gas to the heat exchange unit, wherein the control unit controls the amount of evaporated gas generated in the liquefied gas storage tank The control unit controls the evaporation gas generated in the liquefied gas storage tank to be supplied to the power generation engine and the heat exchange unit by compressing the evaporation gas by the evaporation gas compressor when the amount of the evaporation gas generated in the liquefied gas storage tank The evaporated gas generated in the liquefied gas storage tank may be compressed by the evaporative gas compressor and supplied to the power generation engine.

Specifically, the heat exchanger may be a re-condenser.

Specifically, a pump unit for pressurizing liquefied gas stored in a liquefied gas storage tank; A vaporizer for vaporizing the liquefied gas and supplying it to a customer; And a heat exchange unit for exchanging heat between the evaporation gas generated in the liquefied gas storage tank and the liquefied gas supplied from the pump, wherein at least two of the pump unit and the vaporization unit are provided, Can be provided.

Specifically, at least two pump units or the vaporizing units may be provided, but only one heat exchanging unit may be provided.

The controller may further include a control unit for controlling at least a part of the liquefied gas supplied to the heat exchanging unit to be supplied to the vaporizing unit according to the amount of the evaporating gas generated in the liquefied gas storage tank.

Specifically, the control unit controls the liquefied gas supplied from the pump unit to be supplied to the heat exchange unit when the amount of the evaporation gas generated in the liquefied gas storage tank is greater than the predetermined amount, When the amount of the evaporation gas is less than the predetermined amount, the liquefied gas supplied from the pump unit is bypassed from the heat exchanging unit to be supplied to the vaporizing unit.

Specifically, the re-liquefying branch line bypassing the heat exchanging unit; And a re-liquefaction valve provided on the bypass line, wherein when the amount of evaporation gas generated in the liquefied gas storage tank is greater than a predetermined amount, the control unit decreases the opening of the re- Wherein the control unit controls the liquefied gas supplied from the pump unit to be supplied to the heat exchange unit and increases the opening degree of the liquefaction valve when the amount of the evaporation gas generated in the liquefied gas storage tank is less than the predetermined amount, Bypassing the heat exchanging unit through the heat exchanging unit so that at least a part of the liquefied gas supplied from the pump unit is supplied to the vaporizing unit.

A first line connecting the liquefied gas storage tank and the customer and having the heat exchange unit; A second line branched on the first line at a front end of the heat exchange unit and including a plurality of the pump units; And a third line on the first line, the third line branched in parallel at a rear end of the heat exchange unit and including a plurality of vaporization units.

Specifically, the first line may be a liquefied gas supply line and the regeneration line, and the second line and the third line may be regeneration first to third lines.

Specifically, the heat exchanger may be a re-condenser.

Specifically, it may be a vessel characterized by including the gas regeneration system.

Specifically, the vessel may be a ship (FSRU) having a floating gas storage and regasification facility.

The gas regeneration system according to the present invention and the ship including the same have the effect of maximizing the regeneration efficiency of the liquefied gas.

1 is a conceptual view of a ship having a conventional gas regeneration system.
2 is a conceptual view of a ship having a gas regeneration system according to an embodiment of the present invention.
3 is a conceptual diagram of a gas regeneration system according to the first embodiment of the present invention.
4 is a conceptual diagram of a gas regeneration system according to a second embodiment of the present invention.
5 is a conceptual diagram of a gas regeneration system according to a third embodiment of the present invention.
6 is a detailed view of the vaporization portion of the gas regeneration system according to the embodiment of the present invention.

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

Hereinafter, the liquefied gas may be used to encompass all gaseous fuels generally stored in a liquid state, such as LNG or LPG, ethylene, ammonia, etc. In the case where the gas is not in a liquid state by heating or pressurization, . This also applies to the evaporative gas. In addition, LNG can be used to encompass both NG (natural gas), which is a liquid state, and NG, which is a supercritical state for the sake of convenience. The LNG may be used to mean not only a gas state evaporation gas but also a liquefied evaporation gas .

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

1 is a conceptual view of a ship including a gas regeneration system according to a conventional embodiment.

1, the conventional gas regeneration system 1 includes a liquefied gas storage tank 10, a feeding pump 20, a boosting pump 21, a buffer tank 30, a vaporizer 40, An evaporative gas compressor 50, a first consumer 61, and a second consumer 62.

The conventional gas regeneration system 1 draws the liquefied gas in the liquid state from the liquefied gas storage tank 10 through the feeding pump 20 and supplies it to the temporary storage tank 30 and supplies it from the temporary storage tank 30 The liquefied gas is pressurized to a high pressure by the boosting pump 21 and regenerated by the vaporizer 41 and the heater 42 of the vaporizing unit 40 and then supplied to the first customer 61.

At this time, the evaporated gas generated in the liquefied gas storage tank 10 is pressurized by the evaporative gas compressor 50 and supplied to the second customer 62 for processing.

However, in the gas regasification system 1, a large amount of liquefied gas is regenerated, so that a large amount of evaporation gas is generated, and the fluctuation is also large, so that it is difficult to treat only the second customer 62.

In addition, since the evaporated gas is processed by the second customer 62 instead of the first customer 61, the consumption of the liquefied gas can not be supplied to the true consumer, thereby failing to satisfy the needs of the consumer.

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

The explanatory symbols L1-L3, H, E, S and P denote the liquefaction gas supply line L1, the regeneration line L2, the evaporation gas supply line L3, the hull H, the engine E, The propeller shaft S and the propeller P will be described in detail in the embodiments of the present invention described in FIGS.

FIG. 2 is a conceptual view of a ship having a gas regeneration system according to an embodiment of the present invention, and FIG. 3 is a conceptual diagram of a gas regeneration system according to the first embodiment of the present invention.

2 and 3, the gas regeneration system 2 according to the first embodiment of the present invention includes a liquefied gas storage tank 10, a feeding pump 20, a boosting pump 21, And includes a storage tank 30, a vaporizer 40, an evaporative gas compressor 50, a first customer 61, a second customer 62 and a recondenser 70.

In the embodiment of the present invention, the liquefied gas storage tank 10, the feeding pump 20, the boosting pump 21, the temporary storage tank 30, the evaporator 40, the evaporative gas compressor 50, 61, the second customer 62, and the like use the same reference numerals for convenience and convenience in the conventional gas regeneration system 1, but they do not necessarily refer to the same configurations.

Here, the ship equipped with the gas regeneration system 2 has a hull 100 composed of a bow portion (not shown), a stern portion (not shown), and an upper deck (not shown) The propeller shaft S is propelled by operating the propeller shaft S by transmitting the power produced by the engine E of the engine room (not shown) disposed therein.

In order to enable the liquefied gas to be re-fed at sea and supplied to the land terminal, the ship is provided with a liquefied gas regeneration system (not shown) provided with a gas regeneration system (2) Ship (LNG RV) or floating liquefied gas storage and regasification facility (FSRU).

Hereinafter, the gas regeneration system 2 according to the first embodiment of the present invention will be described with reference to Figs. 2 and 3. Fig.

Prior to describing the individual configurations of the gas regeneration system 2 according to the embodiment of the present invention, the basic flow paths for organically connecting the individual structures will be described. Here, the passage is a passage through which the fluid flows, and may be a line. However, the present invention is not limited thereto.

The embodiment of the present invention may further include a liquefied gas supply line L1, a regasification line L2, an evaporation gas supply line L3, an evaporation gas branch line L4, and a refueling line L5 . Valves (not shown), which are adjustable in opening degree, may be installed in each line, and the supply amount of the evaporation gas or liquefied gas may be controlled according to the opening degree of each valve.

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

The regeneration line L2 is connected to the temporary storage tank 30 and the first consumer 61 and includes a booster pump 21 and a vaporization unit 40 so that the liquefied gas temporarily stored in the temporary storage tank 30 Or the liquefied gas directly supplied from the liquefied gas supply line L 1 may be pressurized by the booster pump 21 and regenerated by the gasification unit 40 to be supplied to the first customer 61.

The evaporation gas supply line L3 connects the liquefied gas storage tank 10 and the second consumer site 62 and includes an evaporative gas compressor 50 to supply the evaporated gas generated in the liquefied gas storage tank 10 And can be supplied to the second customer 62 by being pressurized by the evaporative gas compressor 50.

The evaporation gas branch line L4 can be branched downstream of the evaporation gas compressor 50 on the evaporation gas supply line L3 to be connected to the recondenser 70 and is supplied with the evaporation gas pressurized by the evaporation gas compressor 50 Can be supplied to the recondenser (70).

The re-liquefaction line L5 is connected to the recondenser 70 and the temporary storage tank 30 or to the liquefied gas supply line L1 so that the recycled evaporated gas in the recondenser 70 is supplied to the temporary storage tank (30).

The regeneration line L2, the evaporation gas branch line L4 and the refilling line L5 are connected to the booster pumps 21a, 21b and 21c, the vaporizers 41a, 41b and 41c, the heaters 42a, 42b and 42c (First to third lines L2a, L2b, and L2c), evaporation gas first to third branch lines (first to third lines L2a, L2b, and L2c) to be connected to each of the components of the re-condensers 70a, 70b, L4a, L4b, and L4c), and the re-liquefied first to third lines (L5a, L5b, and L5c).

Hereinafter, the individual configurations that are organically formed by the above-described respective lines L1 to L5 to implement the gas regeneration system 2 will be described.

The liquefied gas storage tank 10 stores liquefied gas to be supplied to the first customer 61. The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, at which time the liquefied gas storage tank 10 may have the form of a pressure tank.

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

The feeding pump 20 is provided on the liquefied gas supply line L1 and is provided inside or outside the liquefied gas storage tank 10 to store the liquefied gas stored in the liquefied gas storage tank 10 in the temporary storage tank 30 ).

Specifically, the feeding pump 20 is provided between the liquefied gas storage tank 10 and the temporary storage tank 30 on the liquefied gas supply line L 1 to supply the liquefied gas stored in the liquefied gas storage tank 10 to the liquefied gas storage tank 10 And can be supplied to the temporary storage tank 30 by pressurizing the car.

The feeding pump 20 can pressurize the liquefied gas stored in the liquefied gas storage tank 10 to 6 to 8 bar and supply it to the temporary storage tank 30. Here, the feeding pump 20 may pressurize the liquefied gas discharged from the liquefied gas storage tank 10 so that the pressure and the temperature may be somewhat higher, and the pressurized liquefied gas may still be in a liquid state.

In this case, the feeding pump 20 may be a submergible pump when it is provided inside the liquefied gas storage tank 10 and may be a pump that is stored in the liquefied gas storage tank 10 when it is installed outside the liquefied gas storage tank 10. May be provided at a position inside the hull (H) lower than the level of the liquefied gas and may be a centrifugal pump.

The boosting pump 21 may be provided between the temporary storage tank 30 and the recondenser 70 on the liquefied gas supply line L1 and may be provided between the liquefied gas supplied from the feeding pump 20 or the temporary storage tank 30 may be supplied to the re-condenser 70 by pressurizing the liquefied gas at 80 to 120 bar.

The boosting pump 21 can pressurize the liquefied gas in accordance with the pressure demanded by the first customer 61 and can be constituted by a centrifugal pump. At this time, the boosting pump 21 is provided with three first to third boosting pumps 21a, 21b and 21c, and can supply the liquefied gas to the first to third re-condensers 70a, 70b and 70c, respectively.

The temporary storage 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 temporary storage tank 30 can receive the liquefied gas stored in the liquefied gas storage tank 10 from the feeding pump 20 through the liquefied gas supply line L1, and temporarily stores the supplied liquefied gas So that the liquefied gas can be separated into a liquid phase and a vapor phase, and the separated liquid phase can be supplied to the boosting pump 21. [

That is, the temporary storage tank 30 temporarily stores the liquefied gas to separate the liquid phase and the vapor phase, and then supplies the complete liquid phase to the boosting pump 21 so that the boosting pump 21 satisfies the effective suction head NPSH So that cavitation in the boosting pump 21 can be prevented.

The temporary storage tank 30 may be connected to the re-liquefaction line L5 to temporarily store the evaporated gas generated in the liquefied gas storage tank 10.

Specifically, the temporary storage tank 30 can receive and temporarily store the re-liquefied evaporated gas from the recondenser 70 via the re-liquefaction line L5. Thus, the temporary storage tank (30) enables the evaporated gas generated in the liquefied gas storage tank (10) to be supplied at least to the first customer (61).

Here, the temporary storage tank 30 may be formed in a pressure vessel type capable of withstanding pressure and can withstand 6 to 8 bar or 6 to 15 bar. Therefore, the temporary storage tank 30 is supplied with the liquefied gas by the boosting pump 21 while maintaining the pressure of about 6 to 8 bar (or even up to 6 to 15 bar) to lower the compression load of the boosting pump 21 There is an effect that can be.

The temporary storage tank 30 is provided with the first and second spray units 311 and 312 and the packing unit 32 so that the liquefied gas temporarily stored and the evaporated gas generated inside the temporary storage tank 30 can be effectively Can be recycled.

The first spray unit 311 may be provided on the upper side of the packing unit 32 and extend from the distal end of the liquefied gas supply line L1 to the interior of the temporary storage tank 30. The liquefied gas supply line L1 To the packing portion 32. The liquefied gas can be supplied to the packing portion 32 through the liquefied gas.

The first spraying unit 311 can increase the contact area between the liquefied gas and the evaporation gas by spraying the liquid liquefied gas and can play a similar role as the packing unit 32. [

The second sprayer 312 may extend from the distal end of the re-liquefaction line L5 to the interior of the temporary storage tank 30 and may be provided below the packing 32, It is possible to inject the liquefied gas supplied through the packing portion 32 downward.

The packing part 32 may be provided at the center of the temporary storage tank 30 so that the liquefied gas supplied onto the liquefied gas supply line L1 and the evaporation gas naturally generated in the temporary storage tank 30 A member such as gravel may be formed inside to widen the surface area of contact. That is, the packing portion 32 forms numerous voids through the gravel formed therein, and the area in which the liquefied gas flows through these voids and is in contact with the evaporation gas can be increased.

Through this, the packing part 32 can increase the heat exchange efficiency between the liquefied gas and the evaporated gas, and re-liquefy the evaporated gas existing in the temporary storage tank 30. [

The vaporizing section 40 is provided on the regeneration line L2 and can re-vaporize the high-pressure liquefied gas discharged from the booster pump 21.

Specifically, the evaporator 40 is provided on the regeneration line L2 between the first consumer 61 and the recondenser 70 and is constituted by the evaporator 41 and the heater 42. The booster pump 21 And then supplies the liquefied gas to the first consumer 61 through the heater 42 by heating the liquefied gas from the first consumer 61 to a desired temperature through the heater 42. [

Since the vaporizer 40 is supplied through the recondenser 70, it is possible to vaporize the liquefied gas preheated by the recondenser 70, thereby saving the supply of the heat source and improving the energy efficiency .

At this time, the vaporizer 40 is provided with the vaporizer 41 and the heater 42 in three of the first to third vaporizers 41a, 41b, 41c and the first to third heaters 42a, 42b, 42c And the first to third re-condensers 70a, 70b and 70c to form the first to third skids Skid 1, Skid 2 and Skid 3.

The vaporizing unit 40 is supplied with the first heat through the heat source circulation line L8 (see FIG. 6), exchanges heat with the liquefied gas to vaporize the liquefied gas, and the first heat exchanged with the liquefied gas is returned to the heat source circulation line L8.

The vaporizing unit 40 may further include a heat source pump 43 (see FIG. 6) and a seawater heat exchanger 44 (see FIG. 6) on the heat source circulation line L8 to continuously supply the heat source to the first fruit have.

At this time, the gasification unit 40 can use Glycol Water, propane, or the like as a first fuel for vaporizing the liquefied gas, and can supply the high-pressure vaporized liquefied gas to the first consumer 61 Can supply.

The following description will be made with reference to Fig. 6 for explaining the detailed configuration of the vaporizing section 40. Fig.

6 is a detailed view of the vaporization portion of the gas regeneration system according to the embodiment of the present invention.

6, the evaporator 40 includes a vaporizer 41, a heater 42, a heat source pump 43, a seawater heat exchanger 44, a nitrogen supplier 45, a phase change material storage device controller The first to third storage devices 91 to 93, and the heat source sharing pump 101, as shown in FIG.

The vaporizing section 40 supplies a heat source to the vaporizer 41 and the heater 42 for vaporizing and heating the liquefied gas and supplies the first fruit (glycol water) to the heat source circulation line L8 through the heat source pump 43, And can transfer the heat source of the seawater to the first fruit through the seawater heat exchanger 44. That is, the heat source is transferred from the seawater to the first fruit and from the first fruit to the liquefied gas to realize the liquefaction of the liquefied gas. Here, the vaporizer 41 may be a printed circuit board type (PCHE).

The vaporization unit 40 may include a first phase change material storage device 91 as a thermal storage device for storing the heat supplied from the first fruit.

The phase change material first storage device 91 can supply the stored heat to the vaporization part 40 when the vaporization part 40 fails to vaporize the liquefied gas through the first heat, And can be connected to the device control unit 81d by wire or wirelessly.

A phase change material (91) is a thermal storage device that stores heat supplied from a first heat source through a phase change material at a normal time for regenerating a liquefied gas through a first heat source, It is possible to dissipate and supply the heat of the phase change material during a period in which the heat is required (a period during which the vaporization part 40 does not vaporize the liquefied gas through the first heat).

 A phase change material is a solid phase in which the phase state changes from solid to liquid at the moment of storing the heat and stores the phase change at the moment when the heat is released. And the like. Such a phase change may have a greater amount of heat than the material exchanged without phase change, and is thus very effective as a thermal buffer.

The phase change material storage device control unit 81d controls the phase change material first storage device 91 and the discharge valve 89a in accordance with the temperature change of the first fruit measured by the first fruit temperature measurement sensor 87 .

The phase change material storage device control unit 81d is connected to the first fruit temperature measurement sensor 87 for measuring the temperature of the first fruit flowing on the heat source circulation line L8 in a wire or wireless manner, And the first fruit can be temporarily stored in the first fruit temporary tank 89b through adjustment of the opening degree of the discharge valve 89a by being connected with the discharge valve 89a by wire or wirelessly.

More specifically, the phase change material storage device control unit 81d stores the phase change material stored in the phase change material first storage device 91 when the temperature of the first fruit measured by the first fruit temperature sensor 87 is lower than the predetermined temperature And controls the supply of the heat to the first heat storage material 91 and stores the heat in the phase change material first storage 91 when the temperature of the first heat measured from the first heat storage temperature sensor 87 is higher than the preset temperature Can be controlled.

At this time, when the temperature of the first fruit measured from the first fruit temperature sensor 87 is lower than the predetermined temperature, the phase change material storage device control unit 81d opens the opening of the discharge valve 89a to open the evaporator 41 ) Is controlled to be supplied to the first fruit temporary tank 89b through the discharge line L15 and the temperature of the first fruit measured from the first fruit temperature measurement sensor 87 is controlled to be lower than the preset temperature It is possible to control to close the opening of the discharge valve 89a.

The phase change material storage unit control unit 81d controls the phase change material storage unit 81d based on the operating state or the inoperable state of the heat source pump 43 measured by the operation detection sensor (not shown) of the heat source pump 43 The storage device 91 and the discharge valve 89a can be controlled.

The phase change material storage device control unit 81d may be connected to an operation detection sensor for measuring whether the heat source pump 43 is operating or not, either wired or wirelessly, to receive operation information of the heat source pump 43, And the first fruit can be temporarily stored in the first fruit temporary tank 89b through adjustment of the opening degree of the valve.

Specifically, when the operating state of the heat source pump 43 transmitted from the operation detection sensor is in an inoperable state, the phase change material storage device control unit 81d stores the heat stored in the phase change material first storage device 91 as a first And to control the phase change material first storage device 91 to store the heat when the operating state of the heat source pump 43 transmitted from the operation detection sensor is in an operating state.

At this time, when the operating state of the heat source pump 43 transmitted from the operation detection sensor is in an inoperable state, the phase change material storage device control unit 81d opens the opening of the discharge valve 89a, When the operation state of the heat source pump 43 transmitted from the operation detection sensor is in an operating state, the first heat storage tank 89b is controlled to supply the first fruit through the discharge line L15 to the first fruit temporary tank 89b, The opening degree can be controlled to be closed.

As a result, in the embodiment of the present invention, it is not necessary to install a separate temperature control device, and when the first fruit reaches a predetermined temperature, the phase change material first storage device 91 causes a phase change to heat the first fruit immediately So that it is possible to prevent damage due to freezing of the first fruit by the liquefied gas cold heat of the evaporator 41 and the heater 42. [

The first phase change material storage device 91 is advantageous in that the construction cost is lower than that of a separate heater or a separate temperature control device, resulting in cost reduction and corresponding time reduction.

The phase change material storage unit control unit 81d controls the nitrogen supply unit 45, the nitrogen supply valve 88a and the nitrogen discharge valve (not shown) in accordance with the temperature change of the first fruit measured from the first fruit temperature sensor 87 88b.

The phase change material storage device control unit 81d is connected to the first fruit temperature measurement sensor 87 for measuring the temperature of the first fruit flowing on the heat source circulation line L8 in a wire or wireless manner, A nitrogen feeder 45 (purging portion) for purging the regasification line L2 on the vaporizer 41, a nitrogen feed valve 88a provided on the nitrogen feed line L9a, A first shutoff valve CV1 provided upstream of the carburetor 41 on the regasification line L2 and a second shutoff valve CV2 provided on the downstream side of the carburetor 41 on the regasification line L2, The second shutoff valve CV2 may be connected to the second shutoff valve CV2 in a wired or wireless manner to supply nitrogen to the nitrogen supply line L9a or to discharge the liquefied gas and nitrogen to the nitrogen discharge line L9b.

Specifically, when the temperature of the first fruit measured by the first fruit temperature sensor 87 is lower than the predetermined temperature, the phase change material storage device control unit 81d controls the nitrogen supply valve 88a and the nitrogen discharge valve 88b And closes the first shutoff valve CV1 and the second shutoff valve CV2 to supply the nitrogen stored in the nitrogen supplier 45 to the regeneration line L2 via the nitrogen supply line L9a, The supplied nitrogen can be controlled so that the liquefied gas on the regasification line L2 is purged and discharged to the outside through the nitrogen discharge line L9b.

The nitrogen supply valve 88a and the nitrogen discharge valve 88b are closed and the first shutoff valve CV1 and the second shutoff valve 88b are closed when the temperature of the first fruit measured from the first fruit temperature sensor 87 is higher than the preset temperature. The shutoff valve CV2 can be opened to control the liquefied gas on the regasification line L2 to flow normally and regenerate

In this embodiment of the present invention, there is no need to install a separate temperature control device, and when the first heat reaches a predetermined temperature, the liquefied gas on the re-oxidation line (L2) is instantly purged through the nitrogen supplier (45) It is possible to prevent breakage due to freezing of the first fruit by the liquefied gas cold heat of the heater 41 and the heater 42. [

In the embodiment of the present invention, the first heat source shared inlet line L10a and the first heat source shared draw line L10b are branched on the heat source circulation line L8, and the first heat source shared first heat exchanger 203, And the second heat source shared inlet line L11a and the second heat source shared drawer line L11b are respectively branched into the first heat source shared inlet line L10a and the first heat source shared drawer line L10b, And the first heat can be supplied to the second heat exchanger 302.

At this time, a heat source sharing pump 101 may be provided on the first heat source common inlet line L10a to supply the first heat to the heat source-shared first heat exchanger 203 or the heat source-shared second heat exchanger 302 .

Therefore, in the embodiment of the present invention, the first fruit cooled by the liquefied gas can be reused as a customer using cold heat, and the energy efficiency in the gas regeneration system 2 is maximized.

An engine cooling system 200 and an air conditioning system 300 may be further included in the embodiment of the present invention and the engine cooling system 200 and the air conditioning system 300 may be provided separately from the first berth, It is a cold / hot supply unit that uses cold heat.

The engine cooling system 200 is a system for cooling the engine E by supplying fresh water to the engine E through the fresh water pump 201 on the fresh water line L12 to cool the engine E, Cooling is performed by supplying the seawater to the clean water heat exchanger 202 through the seawater pump SWP on the seawater line SWL to supply the cool heat or through the heat source sharing first heat exchanger 203 to cool the first fruit Or by supplying cold heat through the phase change material secondary storage device 92. [

In this case, the engine cooling system 200 basically receives cold heat from the first fruit to drive the cooling system, and when the regeneration operation is interrupted, the engine cooling system 200 can receive cooling heat from the seawater in the lane to drive the cooling system. In this case, the first heat and cold heat supply mode and the operation mode in which the cold heat is supplied from the seawater is referred to as a second heat and cold heat supply mode.

The engine cooling system 200 uses the cool heat stored in the phase change material second storage device 92 during the operation mode switching between the first heat supply / cooling heat supply mode and the second heat supply / cooling heat supply mode, The operation can be continued without interruption.

Specifically, in the case of the basic drive (the first heat and cold heat supply mode) in which the engine cooling system 200 receives the cold heat from the first heat and drives the cooling system, clean water flows on the fresh water line L12, The first heat and the fresh water are heat-exchanged through the heat-source-shared first heat exchanger 203, so that the cool heat of the first heat is supplied to the fresh water, and the cooled fresh water is supplied to the engine E.

In the case of the lane-based drive (second heat / cold heat supply mode) in which the regeneration operation is interrupted and the cooling system is driven through the cold / hot supply of the seawater, the phase change material secondary storage 92, And the cold water stored in the phase change material second storage device 92 is used. When the preparation of the cold water for the sea water is completed, the seawater and the fresh water are heat-exchanged through the fresh water heat exchanger 202, Cool heat is supplied to fresh water, and cooled fresh water is supplied to the engine (E). It goes without saying that the above-described configurations can be driven by a separate control unit (not shown).

Here, the engine cooling system 200 can be used not only for the engine E, but also for cooling additional auxiliary equipment (not shown) in the engine room.

The air conditioning system 300 is a system for circulating or cooling air in a space inside the ship and is connected to the cooling first and second lines L13a and L13b and the cooling auxiliary line L14 through a cooling water pump 301, The cooling water is cooled by a chiller using seawater or the cooling water is cooled by a heat source sharing second heat exchanger 302 Or by supplying the cold heat through the third phase change material storage device 93. The phase change material third storage device 93 may be provided in the form of a heat exchanger.

In this case, the air conditioning system 300 basically drives the cooling system by receiving the cold heat from the first fruit, and when the re-generation operation is interrupted, the cooling system is driven by the cold heat supply of the chiller supplied with the cold heat from the sea lane can do. In this case, the first heat and cold heat supply mode and the operation mode in which the cold heat is supplied from the seawater is referred to as a second heat and cold heat supply mode.

The air conditioning system 300 is supplied with the cold heat stored in the phase change material third storage device 93 during the operation mode switching between the first heat supply and cooling mode and the second heat supply and cooling mode, The operation can be continued without interruption.

In the air conditioning system 300, the first and second switching valves 303a and 303b are controlled when the mode is switched between the first and second heat and cold supply modes.

Specifically, in the case of the basic drive (the first heat and cold heat supply mode) in which the cooling system is driven by the cooling heat from the first heat in the air conditioning system 300, the opening of the first switching valve 303a is closed, 2 switching valve 303b is opened to allow the cooling water to flow on the cooling auxiliary line L14 and the cooling first line L13a and the first and the second cooling water flow through the heat source sharing second heat exchanger 302 The cold heat of the first fruit is supplied to the cooling water, and the cooled cooling water is supplied to the air conditioner (HVAC).

In the case of a secondary drive (second heat / cold supply mode) in which the cooling system is driven through the cold supply of the chiller supplied with cold heat from the seawater by interrupting the regenerating operation, during the preparation of the cold supply of the chiller, 3 storage device 93 and the cooling water is used to cool the phase change material in the third storage device 93. When the cold heat supply of the chiller is completed, the opening degree of the first switching valve 303a The opening of the second switching valve 303b is closed and the cooling water flows on the cooling first line L13a and the cooling second line L13b and the sea water and the cooling water are heat exchanged through the chiller, Is supplied to the cooling water, and the cooled cooling water is supplied to the air conditioner (HVAC). It goes without saying that the above-described configurations can be driven by a separate control unit (not shown).

Here, the phase change materials (second and third phase change materials) 92 to 93 are cold storage devices that store the cold heat supplied from the first fruit in the first heat and cold supply mode through the phase change material, Can supply the cold heat of the phase change material during the necessary moment (the drive preparation period of the second heat and cold supply mode during the transition from the first heat and cold supply mode to the second heat / cold supply mode)

 As described above, in the system of the present invention, since the phase change material second and third storage devices (Phase Change Materials) 92 to 93 are provided as the backup devices of the engine cooling system 200 and the air conditioning system 300, So that it is possible to efficiently supply the cold heat of the first fruit to the engine cooling system 200 and the air conditioning system 300, and the reliability of the systems 200 and 300 is maximized.

The evaporation gas compressor 50 can pressurize the evaporation gas generated in the liquefied gas storage tank 10 and supply it to the recondenser 70 or the second customer 62.

Specifically, the evaporative gas compressor 50 is provided on the evaporation gas supply line L3 to pressurize the evaporation gas generated in the liquefied gas storage tank 10 to about 6 to 8 bar or 6 to 15 bar, Or supply it to the second customer 62. At this time, the recondenser 70 can be supplied with the evaporation gas through the evaporation gas branch line L4 branching from the evaporation gas supply line L3.

A plurality of evaporation gas compressors 50 may be provided to press the evaporation gas at multiple stages. For example, three evaporation gas compressors 50 may be provided to pressurize the evaporation gas at three stages. The example three-stage compressor is only one example and is not limited to the three stages.

In the embodiment of the present invention, an evaporative gas cooler (not shown) may be provided at each rear end of the evaporative gas compressor 50. When the evaporation gas is pressurized by the evaporation gas compressor 50, the temperature can also be raised according to the pressure increase. Therefore, in this embodiment, the evaporation gas cooler can be used to lower the temperature of the evaporation gas again. The evaporative gas cooler may be installed in the same number as the evaporative gas compressor 50, and each evaporative gas cooler may be provided downstream of each evaporative gas compressor 50.

Further, in the embodiment of the present invention, when the evaporation gas compressor 50 is provided in parallel and the amount of the evaporation gas generated in the liquefied gas storage tank 10 rapidly increases, When one of the evaporator 50 and the evaporator 50 malfunctions or shut down, the other evaporator gas compressor 50 can be operated to efficiently receive and process the evaporated gas generated in the liquefied gas storage tank 10 .

The first consumer 61 can supply and consume the liquefied gas vaporized by the vaporizing unit 40. Here, the first customer 61 may be a land terminal installed on the land, or a marine terminal floated on the sea, by vaporizing the liquefied gas and supplying and using the gaseous liquefied gas.

The second customer 62 uses the evaporated gas generated from the liquefied gas storage tank 10 as a fuel. That is, the second customer 62 needs evaporation gas and can be driven using the gas as a raw material. The second customer 62 may be, but is not limited to, a generator (e.g., DFDG), a gas-fired unit (GCU), a boiler (e.g.

Specifically, the second customer 62 is connected to the evaporation gas supply line L3 to receive the evaporation gas, and the evaporation gas compressed by the evaporation gas compressor 50 at a low pressure of about 1 to 6 bar (maximum 15 bar) It can be used as fuel.

In addition, the second customer 62 may be a heterogeneous fuel engine capable of using a heterogeneous fuel, so that not only evaporation gas but also oil can be used as the fuel. However, when the evaporation gas and the oil are not mixed and supplied, As shown in FIG. This is to prevent the mixture of two materials having different combustion temperatures from being mixed, thereby preventing the efficiency of the second customer 62 from deteriorating.

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

The recondenser 70 re-liquefies the evaporated gas generated in the liquefied gas storage tank 10 and compressed by the evaporative gas compressor 50 and the liquefied gas supplied from the boosting pump 21 to re-liquefy.

Specifically, the recondenser 70 is provided between the vaporizing section 40 on the regasification line L2 and the temporary storage tank 30 and is connected to the evaporation gas supplied through the vaporizing gas branch line L4 and the regasification line L2 The heat exchanger can heat-exchange the liquefied gas supplied through the heat exchanger.

At this time, the recondenser 70 can supply the vaporized gas, which is heat-exchanged with the liquefied gas and re-liquefied, to the temporary storage tank 30, and the liquefied gas that has been heat-exchanged with the vaporized gas and preheated to the vaporization unit 40.

As such, the gas regeneration system 2 according to the present invention can at least partially process the evaporated gas into the first consumer 61 through the configuration and arrangement of the recondenser 70, thereby effectively meeting the needs of consumers And the treatment of the evaporation gas is more resilient to improve the reliability of the gas regeneration system 2.

Furthermore, since the configuration and arrangement of the recondenser (70) further receive a heat source from the evaporative gas before the liquefied gas is supplied to the evaporator (40), thermal energy for regeneration is saved, thereby maximizing the regeneration efficiency .

Here, the configuration in which the recondenser 70 is heat-exchanged can be a system in which the evaporation gas and the liquefied gas are directly in contact with each other to perform heat exchange, and the evaporation gas and the liquefied gas are supplied into the tube It can be a method of exchanging heat only in between.

Further, the recondenser 70 is formed of a single module with the vaporizing section 40. That is, the recondenser 70 may be formed of one module and one skid with the vaporizer 41 and the heater 42.

Therefore, in the embodiment of the present invention, it is very easy to replace the evaporator if replacement due to malfunction is required through modularization of the evaporator. The reliability of the reboiler system 2 is greatly improved and the evaporator is made compact, It is effective.

At this time, the re-condenser 70 is provided with three first to third re-condensers 70a, 70b, and 70c, and the first to third vaporizers 41a, 41b, and 41c and the first to third heaters 42a, 42b and 42c so as to form the first to third skids Skid 1, Skid 2 and Skid 3.

As described above, the ship having the gas regeneration system according to the present invention has the effect of maximizing the regeneration efficiency of the liquefied gas.

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

4, the gas regeneration system 3 according to the second embodiment of the present invention includes a liquefied gas storage tank 10, a feeding pump 20, a boosting pump 21, a temporary storage tank (not shown) The vaporizer 40, the evaporator gas compressor 50, the first customer 61, the second customer 62, the recondenser 70, the evaporation gas controller 81a, and the liquefied gas controller 81b. .

In the embodiment of the present invention, the liquefied gas storage tank 10, the feeding pump 20, the boosting pump 21, the temporary storage tank 30, the evaporator 40, the evaporative gas compressor 50, 61 and the second customer 62 are the same as or similar to the respective components in the gas regeneration system 2 of the first embodiment of the present invention.

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

In the embodiment of the present invention, the regeneration integrated line L2d and the reflux branch line L6 may be further included.

The reintegration integrated line L2d is connected to the first to third reassembled lines L2a, L2b, and L2c integrally and the other end is connected to the first to third reassembled lines L2a, L2b, and L2c As shown in FIG. That is, the re-integrated line L2d is formed by integrally forming the middle portions of the first to third re-forming lines L2a, L2b, and L2c.

The reintegration integrated line L2d is provided with a recondenser 70 and can supply the liquefied gas supplied from the boosting pump 21 and preheated to supply it to the carburettors 41a, 41b and 41c.

The re-liquefying branch line L6 can be branched and connected in parallel at the re-condensation integration line L2d and is provided with a re-condensation valve 83 at the branch point with the re-condensation integration line L2d to supply the liquefied gas You can control.

The re-condenser 70 is connected to the evaporation gas generated in the liquefied gas storage tank 10 and compressed by the evaporative gas compressor 50 and the liquefied gas supplied from the first to third boosting pumps 21a, 21b and 21c Heat exchange is performed to re-liquefy.

Specifically, the re-condenser 70 is provided on the re-condensation integration line L2d to receive the liquefied gas according to the opening degree of the re-liquefaction valve 83 controlled by the control unit 81, It is possible to re-liquefy the evaporated gas supplied through the line L4.

Here, unlike the configuration of the gas regeneration system 2 according to the first embodiment of the present invention, the recondenser 70 is provided with only one of the evaporation unit 40 without forming a skid, and the evaporation gas control unit 81a By implementing the function of the recondenser 70 according to the amount of evaporated gas through optimized control according to the amount of evaporated gas, the construction cost is reduced, space utilization of the ship (not shown) is improved, 70), so it has a very easy effect.

The evaporation gas control unit 81a controls the evaporation gas supplied to the recondenser 70 according to the amount of the evaporation gas generated in the liquefied gas storage tank 10.

Specifically, when the amount of evaporated gas generated in the liquefied gas storage tank 10 is greater than the predetermined amount, the evaporated gas control unit 81a controls the evaporated gas generated in the liquefied gas storage tank 10 to flow into the evaporated gas compressor 50 To be supplied to the second customer 62 and the re-condenser 70. When the amount of evaporative gas generated in the liquefied gas storage tank 10 is less than the predetermined amount, the liquefied gas storage tank 10 Can be controlled by the evaporative gas compressor 50 to be supplied only to the second customer 62.

The evaporation gas control unit 81a measures the internal pressure of the evaporation gas distribution valve 84 and the liquefied gas storage tank 10 provided at the points where the evaporation gas supply line L3 and the evaporation gas branch line L4 branch off Pressure measuring sensor 85. The internal pressure of the liquefied gas storage tank 10 is received from the internal pressure measuring sensor 85 and the evaporated gas compressor 50 is controlled to supply the evaporated gas After compression, the evaporation gas distribution valve 84 may be controlled to control the direction and amount of movement of the evaporation gas.

The evaporation gas control unit 81a controls the evaporation gas to be supplied to the evaporator 41 by at least partially bypassing the liquefied gas supplied to the recondenser 70 in accordance with the amount of the evaporation gas generated in the liquefied gas storage tank 10 can do. At this time, the evaporation gas control unit 81a may be connected to the re-liquefaction valve 83 by wire or radio, and may perform opening control of each valve, and may include an internal pressure measuring sensor (not shown) for measuring the internal pressure of the liquefied gas storage tank 10 85) can be connected by wire or wireless connection.

Specifically, when the amount of the evaporation gas generated in the liquefied gas storage tank 10 is larger than the predetermined amount, the evaporation gas control unit 81a controls the liquefied gas supplied from the boosting pumps 21a, 21b, The liquefied gas supplied from the boosting pumps 21a, 21b, and 21c is supplied to the re-condenser 70 (70). When the amount of evaporated gas generated in the liquefied gas storage tank 10 is smaller than the predetermined amount, To be supplied to the vaporizers 41a, 41b, and 41c.

The evaporation gas control unit 81a reduces the opening degree of the re-liquefaction valve 83 and supplies the boosting pumps 21a, 21b, 21c, and 21c when the amount of the evaporation gas generated in the liquefied gas storage tank 10 is larger than the predetermined amount. And when the amount of the evaporative gas generated in the liquefied gas storage tank 10 is less than the predetermined amount, the opening degree of the re-liquefaction valve 83 is increased The liquefied gas supplied from the boosting pumps 21a, 21b and 21c can be controlled to be supplied from the recondenser 70 to the vaporizers 41a, 41b and 41c.

The liquefied gas control unit 81b controls the liquefied gas to be supplied to at least one of the first to third boosting pumps 21a, 21b, and 21c according to the flow rate of the liquefied gas discharged from the feeding pump 20.

At this time. In the embodiment of the present invention, the first to third control valves 82a, 82b, 82c and the feeding pump 20 for controlling the supply of liquefied gas to the first to third boosting pumps 21a, 21b, And a flow rate measuring sensor 86 for measuring a flow rate discharged from the flow rate measuring sensor 86. The flow measurement sensor 86 is provided upstream of the temporary storage tank 30 of the liquefied gas supply line L1 in the figure but is provided with a temporary storage tank 30 on the regasification line L2, 21a, 21b, 21c, respectively.

Further, in the embodiment of the present invention, the first to third boosting pumps 21a, 21b, and 21c have different minimum processing flow rates, and the sum of the respective maximum processing flow rates is determined by the first demand source 61 The maximum possible flow rate, that is, the flow rate at which the regasified liquefied gas can be maximally accommodated. The minimum processing flow rate is the minimum flow rate at which the booster pump 21 can operate. When the flow rate below the minimum treatment flow rate flows into the booster pump 21, the booster pump 21 may malfunction or cavitations may occur and the durability may be weakened. If the flow rate is below the minimum treatment flow rate, ) Must be stopped.

For example, the first to third boosting pumps 21a, 21b and 21c in the gas regeneration system 2 according to the first embodiment of the present invention are designed such that the process flow rates are all in the range of 40 to 100 (the minimum process flow rate to the maximum process flow rate In the case of the gas regeneration system 3 according to the second embodiment of the present invention, if the flow rate of the first boosting pump 21a is 60 - 120, the second boosting pump 21b, the processing flow rate of 40 to 100, and the third boosting pump 21c, the processing flow rate of 20 to 80.

 The first boosting pump 21a has a flow rate capable of processing at least the first predetermined flow rate (the minimum processing flow rate is the first predetermined flow rate) and the second boosting pump 21b has the flow rate smaller than the first predetermined flow rate The third boosting pump 21c has a third predetermined flow rate that is smaller than the second predetermined flow rate, and the third flow rate that can be processed (the second predetermined flow rate) (The minimum process flow rate is the third predetermined flow rate). (The first set flow rate> the second set flow rate> the third set flow rate)

The first to third preset flow rates are the minimum flow rates at which the first to third boosting pumps 21a, 21b, 21c can operate with the minimum processing flow rates of the first to third boosting pumps 21a, 21b, 21c.

Specifically, the liquefied gas control unit 81b controls the liquefied gas to be supplied to any one of the first to third boosting pumps 21a, 21b, and 21c when the flow rate of the liquefied gas discharged from the feeding pump 20 is equal to or greater than the first predetermined flow rate When the flow rate of the liquefied gas discharged from the feeding pump 20 is less than the first predetermined flow rate, it can be controlled to be supplied only to the second or third boosting pumps 21b and 21c.

When the flow rate of the liquefied gas discharged from the feeding pump 20 is less than the first predetermined flow rate, the first predetermined flow rate is lower than the second predetermined flow rate (in case of X), the second predetermined flow rate is less than the third predetermined flow rate The second boosting pump 21b and the third boosting pump 21c are controlled so as to be supplied only to the third boosting pump 21b and the third boosting pump 21b, (21c). In case of Z, all the booster pumps (21a, 21b, 21c) must be stopped.

The liquefied gas control unit 81b is connected to the first to third control valves 82a, 82b and 82c and the flow rate measuring sensor 86 by wire or wirelessly, The first to third control valves 82a, 82b and 82c are controlled to control the movement direction and the movement amount of the liquefied gas by receiving the discharge flow rate information of the liquefied gas.

The liquefied gas control unit 81b controls the first to third control valves 82a, 82b, 82c (not shown) when the flow rate of the liquefied gas discharged from the feeding pump 20 transmitted from the flow rate measuring sensor 86 is equal to or greater than the first predetermined flow rate And the flow rate of the liquefied gas discharged from the feeding pump 20, which is transmitted from the flow rate measuring sensor 86, is supplied to the first to third boosting pumps 21a, 21b, The first control valve 82a may be closed and the second and third control valves 82b and 82c may be opened so as to be supplied only to the second or third boosting pumps 21b and 21c .

As described above, in the embodiment of the present invention, malfunctions of the boosting pumps 21a, 21b, and 21c can be effectively prevented through the liquefied gas control unit 81b and the boosting pumps 21a, 21b, 21c can be flexibly coped with, and the driving reliability of the re-ignition system 3 can be greatly improved.

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

5, the gas regeneration system 4 according to the third embodiment of the present invention includes a liquefied gas storage tank 10, a feeding pump 20, a boosting pump 21, a temporary storage tank (not shown) 30, a vaporizer 40, an evaporative gas compressor 50, a first customer 61, a second customer 62, a re-condenser 70, and a booster pump controller 81c.

In the embodiment of the present invention, the liquefied gas storage tank 10, the feeding pump 20, the boosting pump 21, the temporary storage tank 30, the evaporator 40, the evaporative gas compressor 50, 61, the second customer 62, the re-condenser 70, etc. are the same as or similar to the respective components in the gas regeneration systems 2, 3 of the first and second embodiments of the present invention.

Hereinafter, the gas regeneration system 4 according to the third embodiment of the present invention will be described with reference to FIG.

In the embodiment of the present invention, the first and second return lines L7a and L7b and the first and second return valves 87a and 87b may be further included.

The first return line L7a may be branched upstream of the booster pump 21 on the regasification line L2 and connected to the temporary storage tank 30 and the second return line L7b may be connected to the regasification line L2 The booster pump 21 may be branched downstream and connected to the temporary storage tank 30.

The first return valve 87a is provided between the point where the first return line L7a on the regasification line L2 branches and the boosting pump 21 and the second return valve 87b is provided between the regeneration line Condenser 70 and the second return line L7b on the second line L2.

The boosting pump control section 81c controls the liquefied gas supplied to the boosting pump 21 to be supplied to the temporary storage tank 30 when the flow rate of the liquefied gas supplied to the boosting pump 21 is equal to or lower than the preset flow rate, When the flow rate of the liquefied gas supplied to the boosting pump 21 exceeds the preset flow rate, the liquefied gas supplied to the boosting pump 21 is controlled not to be supplied to the temporary storage tank 30.

At this time. In the embodiment of the present invention, it is possible to further include a flow rate measuring sensor 86 for measuring the flow rate discharged from the feeding pump 20. The predetermined flow rate is a minimum flow rate at which the boosting pump 21 can operate Flow rate). When the flow rate below the minimum treatment flow rate flows into the booster pump 21, the booster pump 21 may malfunction or cavitations may occur and the durability may be weakened. If the flow rate is below the minimum treatment flow rate, ) Must be stopped.

The flow measurement sensor 86 is provided upstream of the temporary storage tank 30 of the liquefied gas supply line L1 in the figure but is provided with a temporary storage tank 30 on the regasification line L2, (21).

Specifically, the boosting pump control section 81c closes the first return valve 87a when the flow rate of the liquefied gas supplied from the flow measurement sensor 86 to the boosting pump 21 is equal to or less than the preset flow rate, The liquefied gas supplied to the pump 21 is controlled to be supplied to the temporary storage tank 30 and the flow rate of the liquefied gas supplied to the booster pump 21 transmitted from the flow rate measuring sensor 86 exceeds the preset flow rate The first return valve 87a is opened to control so that the liquefied gas supplied to the boosting pump 21 is not supplied to the temporary storage tank 30. [

More specifically, the boosting pump control section 81c closes the second return valve 87b when the flow rate of the liquefied gas supplied from the flow measurement sensor 86 to the boosting pump 21 is equal to or less than the preset flow rate The boosting pump 21 is stopped to operate so that the liquefied gas supplied to the booster pump 21 is supplied with a predetermined flow rate or more and the liquefied gas supplied from the flow rate sensor 86 to the booster pump 21 The second return valve 87b is opened and the boosting pump 21 is operated so that the liquefied gas supplied to the boosting pump 21 is not supplied to the temporary storage tank 30 but is supplied to the vaporizer 41).

The boosting pump control section 81c can be connected and controlled by the first and second return valves 87a and 87b, the flow measurement sensor 86 and the booster pump 21 in a wired or wireless manner, and the flow measurement sensor 86 The first and second return valves 87a and 87b and the boosting pump 21 may be controlled to control the movement direction and the movement amount of the liquefied gas.

As described above, in the embodiment of the present invention, it is possible to effectively prevent the malfunction of the boosting pumps 21 through the liquefied gas control unit 81b, and to smoothly cope with the operation of the boosting pump 21 to the flow rate of the feeding pump 20 And the driving reliability of the gas regeneration system 4 is greatly improved.

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

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

1: Conventional gas regeneration system 2, 3, 4: Gas regeneration system of the present invention
10: liquefied gas storage tank 20: feeding pump
21: boosting pump 21a: first boosting pump
21b: second boosting pump 21c: third boosting pump
30: Temporary storage tank 311: First spray part
312: second spray part 32: packing part
40: vaporizer 41: vaporizer
41a: first vaporizer 41b: second vaporizer
41c: third vaporizer 42: heater
42a: first heater 42b: second heater
42c: third heater 43: heat source pump
44: Heat source heat exchanger 45: Nitrogen feeder
50: Evaporative gas compressor 61: First demand source
62: second demand point 70: re-condenser
70a: first recondenser 70b: second recondenser
70c: third recondenser 81a: evaporation gas control unit
81b: Liquefied gas control section 81c: Boosting pump control section
81d: phase change material storage device control unit 82a: first control valve
82b: second control valve 82c: third control valve
83: Re-liquefaction valve 84: Evaporative gas distribution valve
85: Internal pressure measuring sensor 86: Flow measuring sensor
87a: first return valve 87b: second return valve
88a: Nitrogen supply valve 88b: Nitrogen discharge valve
89a: discharge valve 89b: first liquor temporary tank
91: phase change material first storage device 911: temperature measurement sensor
92: Second phase change material storage device 93: Third phase change material storage device
101: Heat source sharing pump 200: Engine cooling system
201: Fresh water pump 202: Fresh water heat exchanger
203: heat source sharing first heat exchanger 300: air conditioning system
301: Cooling water pump 302: Heat source sharing second heat exchanger
303a: first switching valve 303b: second switching valve
L1: liquefied gas supply line L2: regasification line
L2a: Regeneration first line L2b: Regeneration second line
L2c: regeneration third line L2d: regeneration integrated line
L3: Evaporative gas supply line L4: Evaporative gas branch line
L4a: Evaporative gas first branch line L4b: Evaporative gas second branch line
L4c: Evaporative gas third line L5: Re-liquefaction line
L5a: Re-liquefied first line L5b: Re-liquefied second line
L5c: Re-liquefied third line L6: Re-liquefied branch line
L7a: first return line L7b: second return line
L8: Heat source circulation line L9a: Nitrogen supply line
L9b: nitrogen discharge line L10a: first heat source shared entry line
L10b: First heat source shared draw line L11a: Second heat source shared entry line
L11b: second heat source shared draw line L12: fresh water line
L13a: Cooling first line L13b: Cooling second line
L14: Cooling auxiliary line L15: Discharge line
CV1: first shutoff valve CV2: second shutoff valve
E: Propulsion engine S: Propeller shaft
P: Propeller H: Hull
Skid: Skid Skid 1: Skid 1
Skid 2: Skid 2 Skid 3: Skid 3
SWL: Sea water line SWP: Sea water pump
HVAC: Air Conditioner Chiller: Chiller (chiller)

Claims (17)

delete delete delete delete delete delete delete A pump unit for pressurizing the liquefied gas stored in the liquefied gas storage tank;
A vaporizer for vaporizing the liquefied gas and supplying it to a customer;
A heat exchanger for exchanging heat between the evaporated gas generated in the liquefied gas storage tank and the liquefied gas supplied from the pump;
A re-liquefying branch line bypassing the heat exchanger; And
And a control unit for controlling at least a part of the liquefied gas supplied to the heat exchanging unit to be supplied to the vaporizing unit according to an amount of the evaporating gas generated in the liquefied gas storage tank,
The pump unit or the vaporizer may further include:
Forming at least two train structures,
The heat-
The pump portion or the vaporizing portion,
Wherein the gas regeneration system is arranged to integrate the liquefied gas flow between the pump section and the vaporization section. 9. The method of claim 8,
Wherein at least two of the pump unit and the vaporizing unit are provided, and only one heat exchanging unit is provided. delete 10. The apparatus according to claim 9,
Wherein the control unit controls the liquefied gas supplied from the pump unit to be supplied to the heat exchange unit when the amount of the evaporation gas generated in the liquefied gas storage tank is greater than the predetermined amount,
Wherein the control unit controls the liquefied gas supplied from the pump unit to be bypassed from the heat exchanging unit and supplied to the vaporizing unit when the amount of evaporating gas generated in the liquefied gas storage tank is less than a predetermined amount. 12. The method of claim 11,
Further comprising a re-liquefaction valve provided on the redistribution branch line,
Wherein,
Wherein when the amount of the evaporative gas generated in the liquefied gas storage tank is greater than the predetermined amount, the opening degree of the re-liquefaction valve is reduced to control the liquefied gas supplied from the pump unit to be supplied to the heat-
Liquefaction valve by bypassing the re-liquefaction branch line through the re-liquefaction branch line when the amount of the evaporation gas generated in the liquefied gas storage tank is smaller than the predetermined amount, So that at least a part of the gas is supplied to the vaporizing portion. 13. The method of claim 12,
A first line connecting the liquefied gas storage tank with the customer and having the heat exchange unit;
A second line branched on the first line at a front end of the heat exchange unit and including a plurality of the pump units; And
Further comprising: a third line on the first line, the third line branched in parallel at a rear end of the heat exchange unit and having a plurality of vaporizers. 14. The method of claim 13,
Wherein the first line is a liquefied gas supply line and a regasification line,
And the second line and the third line are the first to third lines of regeneration. The heat exchanger according to claim 8,
Wherein the recondenser is a recondenser. A vessel comprising the gas regeneration system of any one of claims 8, 9, 11, 15, 17. The method of claim 16,
Characterized in that the vessel is a ship (FSRU) having a floating gas storage and regasification facility.

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