KR20190031079A - Regasification System of liquefied Gas and Ship Having the Same - Google Patents

Abstract

The present invention relates to a liquefied gas regasification system and a ship having the same. The liquefied gas regasification system includes: a liquefied gas supply pump pressurizing liquefied gas discharged from a liquefied gas storage tank; a vaporizer vaporizing the liquefied gas pressurized in the liquefied gas supply pump into a heat medium to supply the same to a demand source; an inline mixer mixing boil off gas and liquefied gas discharged from the liquefied gas storage tank to transmit the mixture to the liquefied gas supply pump; and an auxiliary pump provided between the inline mixer and the liquefied gas supply pump and compensating for a pressure difference between the liquefied gas detouring the inline mixer to be transmitted to the liquefied gas supply pump and the mixed gas passing through the inline mixer to be transmitted to the liquefied gas supply pump.

Description

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

The present invention relates to a liquefied gas regeneration system and a ship having the system.

Recently, as environmental regulations are strengthened, the use of liquefied natural gas (Liquefied Natural Gas), which is close to eco-friendly fuel among various fuels, is increasing. Liquefied natural gas is typically transported through an LNG carrier, where the liquefied natural gas can be stored in a tank of LNG carriers in a liquid state at temperatures below -162 ° C at 1 atm. Liquefied natural gas can be transported in a liquid state because the volume of the natural gas is reduced to one-sixth of that of the gas state.

However, liquefied natural gas is generally consumed in a gaseous state rather than in a liquid state, so that liquefied natural gas stored and transported in a liquid phase needs to be regenerated, and a regenerating system is used.

At this time, the regeneration facility may be mounted on a ship such as LNG carrier, FLNG, FSRU, or the like, and the regeneration facility realizes regeneration by heating liquefied natural gas using a heat source such as seawater.

However, since the liquefied natural gas is in a cryogenic temperature close to -160 degrees, if the temperature difference between the heat source and the heat source becomes large, the durability and the like of the heat exchanger for heating the liquefied natural gas may occur. In addition, when liquefied natural gas is heated using seawater, corrosion of the heat exchanger may occur.

Recently, many researches and developments have been made in order to simplify the regeneration facilities while stabilizing the various components in the process of regenerating the liquefied natural gas stored in the liquid phase.

SUMMARY OF THE INVENTION The present invention has been made to solve the problems of the prior art as described above, and it is an object of the present invention to provide an inline mixer which can reduce a pressure loss by using a type of a fruit heater in which a fruit is stored in a liquid phase, A liquefied gas regeneration system provided with a liquefied gas regeneration system capable of enhancing the placement efficiency, regulating the pressure in the expansion drum in which the fruits are temporarily stored, and / or preventing the fruit from being unnecessarily discharged to the outside .

A liquefied gas regeneration system according to an aspect of the present invention includes: a liquefied gas supply pump for pressurizing liquefied gas discharged from a liquefied gas storage tank; A vaporizer for vaporizing the pressurized liquefied gas by the liquefied gas supply pump and supplying it to a customer; An inline mixer for mixing the vaporized gas and the liquefied gas discharged from the liquefied gas storage tank and delivering the liquefied gas to the liquefied gas supply pump; And an in-line mixer which is provided between the in-line mixer and the liquefied gas supply pump, and which bypasses the in-line mixer and is supplied to the liquefied gas supply pump, And an auxiliary pump for compensating for the difference.

Specifically, the inline mixer may replace a suction drum provided between the liquefied gas storage tank and the liquefied gas supply pump.

Specifically, an evaporative gas supply line connected to the in-line mixer in the liquefied gas storage tank; A liquefied gas supply line connected from the liquefied gas storage tank to the customer via the liquefied gas supply pump; A liquefied gas branch line branched from the liquefied gas supply line upstream from the liquefied gas supply pump and connected to the inline mixer; And a mixed gas supply line connected to the liquefied gas supply line or the liquefied gas supply pump through the auxiliary pump in the inline mixer.

Specifically, it may further comprise a low pressure evaporative gas compressor provided on the evaporative gas supply line.

Specifically, the evaporative gas bypass line bypassing the vaporizer in the liquefied gas storage tank and connected to the customer; And a high pressure evaporative gas compressor provided on the evaporative gas bypass line.

Specifically, the auxiliary pump pressurizes the liquefied gas discharged from the in-line mixer by the pressure lowered by mixing with the evaporation gas while the liquefied gas discharged from the liquefied gas storage tank passes through the inline mixer, Gas feed pump.

Specifically, the apparatus further includes a mixed gas pressure sensor provided in the mixed gas supply line, and the auxiliary pump can be operated in accordance with the measured value of the mixed gas pressure sensor.

A ship according to one aspect of the present invention is characterized by having the liquefied gas regeneration system.

The liquefied gas regeneration system and the ship having the liquefied gas regeneration system according to the present invention are characterized in that when the phase-changeable heat is used for heat exchange with the liquefied gas, the fruit is stored in a liquid phase, By using the heater, the pressure loss can be minimized and the liquefied gas vaporization efficiency can be increased.

The liquefied gas regeneration system according to the present invention and the ship having the liquefied gas regeneration system according to the present invention include an inline mixer to omit the suction drum provided on the hull to ensure visibility and to omit the control system required for the suction drum Can be obtained.

The liquefied gas regeneration system according to the present invention and the ship having the liquefied gas regeneration system according to the present invention return the fruit between the fruit pump and the fruit heater so as to control the pressure of the expansion drum in which the fruit is temporarily stored, The heat exchange efficiency between the liquefied gas and the heat source and the heat exchange efficiency between the heat source and the heat source can be improved.

The liquefied gas regeneration system according to the present invention and the ship having the liquefied gas regeneration system according to the present invention are provided with a liquefied storage tank connected to an expansion drum, and heat of the vapor generated in the lyse storage tank is returned to heat exchange with the liquefied gas, And it is possible to suppress unnecessary external emission of the fruit.

1 is a conceptual diagram of a liquefied gas regeneration system according to a first embodiment of the present invention.
2 is a cross-sectional view of a heater according to a first embodiment of the present invention.
FIG. 3 is a perspective view of a heater according to a first embodiment of the present invention. FIG.
4 is a conceptual diagram of a liquefied gas regeneration system according to a second embodiment of the present invention.
5 is a conceptual diagram of a liquefied gas regeneration system according to a third embodiment of the present invention.
6 is a conceptual diagram of a liquefied gas regeneration system according to a fourth embodiment of the present invention.

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

Hereinafter, the liquefied gas may be LPG, LNG, or ethane, and may be, for example, LNG (Liquefied Natural Gas), and the evaporation gas may refer to BOG (Boil Off Gas) such as natural vaporized LNG.

Also, the liquefied gas may be used in the following terms to encompass both a liquid state, a natural vaporized state, and a forced vaporized state, although the term "vaporized gas" can be used to mean a gas that is spontaneously vaporized in a liquefied gas storage tank .

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. Hereinafter, the liquefied gas regeneration system of the present invention will be described, and the present invention includes a liquefied gas regeneration system and a vessel having the liquefied gas regeneration system. However, at this time, it is noted that the ship is an expression that covers marine plants such as FLNG and FSRU in addition to commercial vessels.

Also, in the following, high pressure may mean more than 100 bar, and low pressure may mean less than 30 bar, but it should be noted that expressions such as high or low pressure are relative, but not absolute.

FIG. 1 is a conceptual diagram of a liquefied gas regeneration system according to a first embodiment of the present invention, FIG. 2 is a sectional view of a luminescent heater according to a first embodiment of the present invention, and FIG. 3 is a cross- Fig.

1 to 3, a liquefied gas regeneration system 1 according to a first embodiment of the present invention includes a liquefied gas storage tank 10, a suction drum 20, a liquefied gas supply pump 30, A vaporizer 40, and a fruit supply unit 50.

The liquefied gas storage tank 10 stores a liquefied gas in a liquid state. The liquefied gas stored in the liquefied gas storage tank 10 is discharged to the outside of the liquefied gas storage tank 10 and then supplied to the vaporizer 40. The liquefied gas stored in the liquefied gas storage tank 10 can be stored in the liquefied gas storage tank 10, And can be delivered to the customer 60.

At this time, the customer 60 may be an engine or a turbine producing energy, or may be a city gas, a general household, or the like, but is not particularly limited, and the liquefied gas may be delivered to the customer 60 in a vaporized state by the vaporizer 40 have.

A plurality of liquefied gas storage tanks 10 may be provided and may be arranged side by side in the hull 3. For example, as shown in the figure, at least four liquefied gas storage tanks 10 may be disposed in a predetermined direction (forward and backward directions) inside the hull 3, but the number or arrangement of the liquefied gas storage tanks 10 may be limited It is not.

The liquefied gas storage tank 10 has a transfer pump 11 therein. The transfer pump 11 may be installed as a submerged pump so as to be submerged in the liquefied gas stored in the liquefied gas storage tank 10.

The transfer pump 11 discharges the liquefied gas stored in the liquefied gas storage tank 10 to the outside of the liquefied gas storage tank 10. At this time, the liquefied gas can be slightly pressurized by the transfer pump 11, Pressurization by the pump 11 may not be performed up to the required pressure of the customer 60. Therefore, the liquefied gas supply pump 30 pressurizes the liquefied gas by the difference between the pressure of the liquefied gas pressurized by the transfer pump 11 and the required pressure of the customer 60.

A liquefied gas supply line 12 may be provided from the transfer pump 11 to the customer 60. A suction drum 20, a liquefied gas supply pump 30, a vaporizer 40 and the like may be provided.

The suction drum 20 temporarily stores the liquefied gas. Since the transfer pump 11 provided in the liquefied gas storage tank 10 is kept in a state of being immersed in the liquefied gas, there is no possibility of causing a cavitation problem due to the fear of inflow of the evaporated gas. However, This is not the case in the case of the liquefied gas supply pump 30 provided outside.

Therefore, the suction drum 20 temporarily stores the liquefied gas discharged from the liquefied gas storage tank 10 while temporarily storing the liquefied gas in the liquefied gas storage tank 10 so that the gaseous state does not coexist in the liquefied gas flowing into the liquefied gas supply pump 30 It is possible to prevent the occurrence of cavitation in the liquefied gas supply pump 30 by transmitting it to the liquefied gas supply pump 30.

The suction drum 20 is provided with a liquefied gas supply pump 30 for supplying the liquefied gas delivered from the feed pump 11 to match the effective suction head NPSHr to be supplied to the liquefied gas supply pump 30 The liquefied gas having the effective suction head or more can be delivered to the liquefied gas supply pump 30.

The suction drum 20 is in the form of a tank having a certain space, and may have means for regulating the internal pressure. The evaporation gas supply line 13 is connected from the liquefied gas storage tank 10 to the suction drum 20 so that the gaseous evaporative gas generated in the liquefied gas storage tank 10 is injected into the suction drum 20 The pressure of the suction drum 20 can be increased.

The suction drum 20 may further include a pressing unit 21 for injecting a gas such as nitrogen into the suction drum 20 to increase the internal pressure of the suction drum 20. However, ) Is not particularly limited.

The liquefied gas return line 31 is branched at the liquefied gas supply line 12 downstream of the liquefied gas supply pump 30 and the liquefied gas return line 31 is branched from the liquefied gas return line 31, So that the internal pressure of the suction drum 20 can be increased through the recovery of the liquefied gas by the liquefied gas return line 31. [

The suction drum 20 may be provided with a liquefied gas discharge line 22 and the liquefied gas discharge line 22 may be provided with the suction drum 20 to prevent the suction drum 20 from being excessively pressurized. A safety valve (not shown) that automatically opens when the internal pressure exceeds a certain level may be provided.

The liquefied gas discharged by the liquefied gas discharge line 22 may be discharged to the atmosphere, or may be returned to the liquefied gas storage tank 10, and may be discharged to various locations other than that which is not limited.

As described above, the suction drum 20 temporarily stores the liquefied gas delivered from the transfer pump 11 of the liquefied gas storage tank 10, while maintaining the internal pressure constant, and supplies the liquefied gas to the liquefied gas supply pump 30 It is possible to ensure the stability of operation of the liquefied gas supply pump 30 by making the pressure constant while the gas satisfies the effective suction head.

In order to control the internal pressure of the suction drum 20, mixing of the evaporation gas, inflow of the gaseous material, return of the pressurized liquefied gas, and the like are performed by measuring the internal pressure of the suction drum 20 with a pressure sensor It is obvious that the valve can be controlled by controlling the valve (not shown) according to the measured value.

The liquefied gas supply pump (30) pressurizes the liquid liquefied gas discharged from the suction drum (20). The liquefied gas pressurized by the liquefied gas supply pump 30 may be equal to or higher than the required pressure of the customer 60 and there may be no means for further pressurizing the liquefied gas between the liquefied gas supply pump 30 and the customer 60 .

The liquefied gas return line 31 mentioned above may be provided downstream of the liquefied gas supply pump 30 and the pressure of the suction drum 20 may be improved through the liquefied gas return line 31. [

The liquefied gas return line 31 does not return the liquefied gas pressurized by the liquefied gas supply pump 30 to the suction drum 20, It may be a line that circulates the minimum flow.

In the latter case, the liquefied gas return line 31 is connected at the middle end of the liquefied gas supply pump 30, not at the outlet end (or downstream of the outlet end) of the liquefied gas supply pump 30, , The low-pressure liquefied gas that has simply passed through the liquefied gas supply pump 30 without being pressurized can be returned to the suction drum 20 and can be independent of the internal pressure control of the suction drum 20. [

Of course, the present embodiment includes a liquefied gas return line 31 for returning high-pressure liquefied gas to the suction drum 20 to increase the pressure of the suction drum 20, and an operation for maintaining the operation of the liquefied gas supply pump 30 A liquefied gas return line 31 for circulating the low-pressure liquefied gas at the minimum flow rate to the suction drum 20 at a time can be provided at the same time.

The vaporizer (40) vaporizes the liquefied gas. The vaporizer 40 may be provided in the liquefied gas supply line 12 and may heat the liquefied gas using various fruits. For example, the present embodiment may be applied to a case where the glycol water, which does not cause corrosion of a heat exchanger, Propane which can utilize latent heat for heat exchange, R134a, CO2, R218 and the like can be used.

Hereinafter, for convenience, the fruit used in the carburetor 40 is phase-changed from a gas phase to a liquid phase by the liquefied gas in the vaporizer 40, and a heat source (steam, fresh water, Seawater or the like) that has a physical property that changes phase from a liquid phase to a gas phase.

The vaporizer 40 may have a two-stream structure having a flow path through which the liquefied gas flows and a flow path through which the liquid flows, and the flow path through which the liquefied gas flows may be connected in parallel with the liquefied gas supply line 12 in which the vaporizer 40 is installed . The flow path through which the fruit flows can be connected to the fruit circulation line 54 of the fruit supplying part 50 in parallel.

The temperature of the liquefied gas vaporized by the vaporizer 40 may be a required temperature of the consumer 60 and may vary depending on the type of the consumer 60. The temperature of the liquefied gas heated by the vaporizer 40 is particularly limited I never do that. However, the vaporizer 40 can vaporize the liquefied gas by heating the liquefied gas to about 10 to 50 degrees, for example, and supply it to the consumer 60.

The fruit supplying section 30 supplies the fruit to the vaporizer 40. [ In this case, as described above, the fruit is a substance that is phase-changed by heat exchange with the liquefied gas in the vaporizer 40, and the fruit supplying unit 30 includes the fruit pump 51, the fruit heater 52, 53).

The fruit pump (51) transfers the fruit to the vaporizer (40). The fruit pump 51 may be provided for flow of the fruit, and the fruit may be slightly pressurized to increase heat exchange efficiency.

The plurality of the fruit pumps 51 may be provided in parallel, and at least one of them may be driven to the main and the other one may be driven by auxiliary or backup.

The fruit heater (52) heats the fruit. The fruit heater (52) can heat the fruit using a heat source such as seawater. A heat source supply line 5221 may be connected to the heat source 52. The heat source supply line 5221 may include a heat source pump 5222 for supplying the heat source to the heat source heater 52, A heat source supply valve 5223 for adjusting the supply flow rate of the heat source according to the temperature of the heat in the upstream and / or downstream, and the like.

For example, when the heat source is seawater, the heat source supply line 5221 can transfer seawater from the outside (for example, a seed chest) to the fruit heater 52, while heating the fruit in the fruit heater 52, It can be discharged to the outside (for example, a seed chest) after being subjected to a treatment such as heating or sterilization, if necessary. That is, the heat source supply line 5221 may allow seawater to circulate between the seed chest and the fruit heater 52, but may not be in a closed loop form.

Of course, in the present embodiment, in addition to the seawater, the heaters 52 can utilize various kinds of heat sources such as steam, clean water, engine exhaust, engine cooling water, and various waste heat generated from the ship.

Referring to FIGS. 2 and 3, the heater 52 of the present embodiment may be provided in a different type from the vaporizer 40. Specifically, the fruit heater 52 stores the liquid fruit, has a structure that the fruit heat-exchanged with the liquefied gas flows, and the heat is heated while the heat source flows into the fruit of the liquid. For this, the fruit heater 52 may have a housing 521, a heat source supply unit 522, a shielding film 523, a filling member 524, a discharge unit 525, and a support 526.

The housing 521 stores the liquid phase liquid at a predetermined level. The housing 521 may have a cylindrical shape in which the housing 521 is laid down. The housing 521 has a fruit inlet 5211 through which the liquid heat exchanged with the liquefied gas flows, a fruit outlet 5212 through which the vapor in the gas phase heated by the heat source is discharged, Lt; / RTI >

The fruit inlet 5211 may be located above the liquid level of the liquid fruit stored in the housing 521 so that the liquid fruit liquefied by the liquefied gas may be introduced into the housing 521 in a sprinkled form have.

The fruit outlet 5212 discharges the gaseous phase out of the housing 521 and may be provided at the upper end of the housing 521. However, a blocking film 523 may be provided so that the liquid fruit is not discharged to the fruit outlet 5212.

The heat source supply unit 522 includes a heat source supply line 5221 through which a heat source flows into the liquid heat stored in the housing 521 and a heat source flows and a heat source supply line 5221, As shown in FIG.

At this time, the heat sink 5224 may have a shape of a disk or the like, and may be arranged on the heat source supply line 5221 having a U-shaped shape that is laid down in parallel with a plurality of spaced apart from each other according to the flow direction of the heat source.

The liquid in the liquid phase may be stored in the housing 521 by an amount such that at least a part of the heat sink 5224 is always locked, so that the liquid heat is vaporized by the heat radiated from the submerged heat sink 5224 , It can be phase-changed into the fruit of the weather.

For example, the lower dotted line in FIG. 2 is the minimum height of the liquid level formed by the liquid phase stored in the housing 521, and the upper dotted line may be the maximum height of the liquid level. That is, in a state where at least the fruit heater 52 is in operation, the liquid level formed in the housing 521 can be placed between the two dotted lines in Fig.

The liquid heat of the liquid that flows into the housing 521 through the heat inlet 5211 flows upward from the liquid surface of the liquid heat stored in the housing 521. The heat sink 5224 is immersed in the liquid heat And may be positioned below the fruit inlet 5211. [ Accordingly, the fruit supplying part 50 can vaporize the liquid-phase fruit stored in the housing 521 first, instead of directly vaporizing the fruit introduced into the housing 521 after heat-exchanged with the liquefied gas and liquefied.

The heat sink 5224 may have a disk shape similar to the circular shape of the section of the housing 521. [ However, the heat sink 5224 may have a cross section smaller than the cross section of the housing 521, and may be provided below the center of the housing 521 so as to be kept in a state of being submerged in the liquid heat stored in the housing 521.

In this case, liquid heat may be stored in the housing 521 on the left and right sides of the heat sink 5224. Since the heat adjacent to the inner wall of the housing 521 is located away from the heat sink 5224, A filling member 524 to be described later may be provided to reduce the internal space of the housing 521 so as to reduce the distance between the heat and the heat sink 5224. [

The blocking film 523 is located above the liquid surface of the liquid phase stored in the housing 521 in the housing 521 and blocks the liquid phase liquid from being discharged to the liquid outlet 5212. The shielding film 523 may be provided between the fruit outlet 5212 and the fruit inlet 5211 and may be formed in various forms without limitation so as to inhibit the rise of the fruit in the liquid phase.

Particularly, when the liquid phase liquid liquefied by the liquefied gas flows in through the inflow port 5211 located above the liquid phase stored in the housing 521, the liquid film falling on the liquid surface is splashed It is possible to shut off the inflow into the fruit outlet 5212.

The filling member 524 is provided on the inner wall of the housing 521 in the vicinity of the heat sink 5224. [ The filler member 524 may be formed in the interior of the housing 521 in order to reduce the distance between the liquid heat and the heat sink 5224 and also to keep the liquid level of the liquid fruit at a sufficient height, It can be arranged to be forcibly reduced.

Of course, if the distance between the heat sink 5224 and the liquid phase in the housing 521 is not a significant problem for the vaporization of the heat, the filler member 524 can be deformed or omitted in any way. For example, when the heat sink 5224 is elliptic with a width larger than the height, the distance between the heat adjacent to the inner wall of the housing 521 and the heat sink 5224 is not large, so that the filling member 524 can be omitted.

The discharge unit 525 may be provided to discharge the liquid heat stored in the housing 521 to the outside in an emergency situation or the like and may be provided at the lower end of the housing 521 to drain the liquid heat.

The support 526 is provided to support the housing 521. At least one support 526 is provided on the outer wall of the housing 521 and may have a leg shape or the like. Of course, the shape and arrangement of the supporter 526 are not particularly limited, but may be provided so as not to interfere with the discharge of the heat by the discharge portion 525.

As described above, the heaters 52 of the present embodiment vaporize the heat by using the heat sink 5224 that is locked to the liquid heat, and the heat that has been cooled by the liquefied gas flows from the upper portion of the housing 521 521, respectively. Thus, the present embodiment can minimize the pressure loss occurring in the closed loop in which the heat is circulated when the liquefied gas is regenerated with the heat using the latent heat.

Generally, the lower the injection pressure is, the more advantageous the filler heater 52 is, and the higher the injection pressure in the vaporizer 40, the more advantageous it is. Therefore, if the pressure loss generated by the raw material heater 52 is small, the system can be configured effectively.

Therefore, the heat source heater 52 of the present embodiment has a structure in which the housing 521 is filled with the heat of the vaporized state vaporized by the heat radiation plate 5224 so as to have a pressure higher than a predetermined pressure, (For example, the pressure loss is less than 2 kPa), the heat transfer area can be supplied only to the liquid phase having a good heat exchange efficiency, and the size and the price of the liquid heater 52 can be reduced.

Accordingly, in the present embodiment, the heat exchange efficiency can be improved by increasing the pressure of the heat that flows into the vaporizer 40, and thus the size of the vaporizer 40 can be reduced and the cost can be reduced.

Particularly, the liquefied gas regeneration system 1 has the largest cost in the price of the vaporizer 40, so that the present embodiment can have a cost saving effect of the liquefied gas regeneration system 1 itself.

The expansion drum 53 temporarily stores the fruit. The expansion drum 53 may have the form of a tank for storing the fruit and can ensure the flow rate of the fruit supplied to the vaporizer 40.

The expansion drum 53 may be provided with a drum pressure sensor 531 for measuring the internal pressure and a safety valve (not shown) provided in the expansion drum 53 when the internal pressure of the expansion drum 53 is excessively high Is opened so that the fruit can be discharged to the outside of the expansion drum (53).

Conversely, the expansion drum 53 can be replenished with heat from the outside. Even though the loss of the fruit is hardly caused by the fact that the fruit is circulated in the closed loop, in order to replenish the fruit due to the unexpected leakage of the fruit, or to discharge and supplement the fruit for the maintenance of the fruit, Can be used.

The fruit pump 51 and the fruit heater 52 and the expansion drum 53 can be connected through a closed loop of the fruit circulation line 54 and the fruit is connected to the expansion drum 53, the fruit pump 51, (52) to the vaporizer (40), and then recovered to the expansion drum (53).

For this, the fruit circulation line 54 may have a closed loop structure for sequentially connecting the expansion drum 53, the fruit pump 51, the fruit heater 52, and the evaporator 40, and the fruit circulation line 54 A heat temperature sensor 541 for checking the temperature of the heat can be provided upstream of the heaters 52 and downstream of the heaters 40. [

At this time, the measured value by the fruit temperature sensor 541 can be used for control of the fruit pump 51, the heat source supply valve 5223, and the like, and also used for control of the feed pump 11, liquefied gas supply valve, Of course.

As described above, according to the present embodiment, the heaters 52 are provided in a structure minimizing the pressure loss, thereby reducing the size of the vaporizer 40 by reducing the heat exchange efficiency in the vaporizer 40, Can be increased.

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

4, a liquefied gas regeneration system 1 according to a second embodiment of the present invention includes a liquefied gas storage tank 10, a liquefied gas supply pump 30, a vaporizer 40, and the like, In addition, an inline mixer 70 may be provided to omit the suction drum 20.

Hereinafter, the present embodiment will be described mainly in terms of differences from the previous embodiment, and it is also noted that the same applies to the third and fourth embodiments described later.

The in-line mixer 70 mixes the evaporation gas and the liquefied gas discharged from the liquefied gas storage tank 10 and transfers the mixture to the liquefied gas supply pump 30. The inline mixer 70 replaces the suction drum 20 described in the first embodiment and performs the function of liquefying the evaporated gas generated in the liquefied gas storage tank 10 with the liquefied gas in the same manner as the suction drum 20 .

Unlike the suction drum 20 provided on the liquefied gas supply line 12 between the liquefied gas supply pumps 30 in the liquefied gas storage tank 10, the inline mixer 70 is provided in the liquefied gas storage tank 10 may be provided in parallel with the liquefied gas supply line 12 instead of being provided in the liquefied gas supply line 12 between the liquefied gas supply line 12 and the liquefied gas supply pump 30.

In this case, the in-line mixer 70 can be connected to the liquefied gas branch line 71 branched from the liquefied gas supply line 12, and the liquefied gas branch line 71 can be connected to the liquefied gas supply line 12, May be branched from the upstream of the pump 30 and connected to the inline mixer 70.

Therefore, the in-line mixer 70 can receive some of the low-pressure liquefied gas supplied from the liquefied gas storage tank 10 to the liquefied gas supply pump 30 through the liquefied gas branch line 71. At this time, various measurement means such as a liquefied gas temperature sensor 711 and / or a liquefied gas flow rate sensor 712 for measuring the state of the liquefied gas flowing into the inline mixer 70 are provided on the liquefied gas branch line 71 .

Unlike the liquefied gas supply line 12, the evaporation gas supply line 13 may be connected directly to the in-line mixer 70 in the liquefied gas storage tank 10. The evaporation gas supply line 13 conveys the evaporation gas generated in the liquefied gas storage tank 10 to the inline mixer 70. The present embodiment includes a low pressure evaporative gas compressor 13 can be provided.

In the case of the suction drum 20, it is possible to control the internal pressure to be increased, but in the case of the inline mixer 70, it is impossible to control the internal pressure rise or the like. Therefore, the present embodiment compresses the evaporation gas supplied from the liquefied gas storage tank 10 to the in-line mixer 70 to the low-pressure evaporative gas compressor 13 to ensure the same function as the pressure regulation in the suction drum 20 . An evaporation gas flow rate sensor 132 and / or an evaporation gas temperature sensor 133 may be provided in the evaporation gas supply line 13 in order to control the operation of the low-pressure evaporation gas compressor 13.

The in-line mixer 70 is configured to discharge the evaporated gas discharged from the liquefied gas storage tank 10 and compressed by the low-pressure evaporative gas compressor 13 from the liquefied gas storage tank 10 to the liquefied gas supply pump 30 It may be liquefied by mixing with a part of the liquefied gas branched before being introduced, and a state in which the liquefied gas is mixed with the evaporation gas may be referred to as a mixed gas herein. It should be noted that the gas mixture may be in a liquid phase, but the vapor phase may be mixed because the vapor gas will be liquefied by mixing with the liquefied gas.

The in-line mixer 70 is connected to the liquefied gas supply line 12 and / or the liquefied gas supply line 12 from the in-line mixer 70 to deliver the mixed gas to the liquefied gas supply line 12 and / And a mixed gas supply line 72 connected to the supply pump 30.

In the mixed gas supply line 72, an auxiliary pump 80 may be provided. The auxiliary pump 80 is provided between the in-line mixer 70 and the liquefied gas supply pump 30 on the basis of the flow of the liquefied gas (or the mixed gas), and can compensate the pressure difference between the liquefied gas and the mixed gas.

The liquefied gas is discharged from the liquefied gas storage tank 10 to the liquefied gas discharged from the liquefied gas storage tank 10 and delivered to the liquefied gas supply pump 30 bypassing the inline mixer 70 through the liquefied gas supply line 12. [ The mixed gas, which is introduced into the in-line mixer 70 through the liquefied gas branch line 71 and mixed with the evaporated gas and then delivered to the liquefied gas supply pump 30, may be slightly lowered in pressure due to the mixing of the evaporated gas have.

Therefore, in the present embodiment, the auxiliary pump 80 for pressurizing the mixed gas can be provided, so that the pressure difference between the mixed gas and the liquefied gas introduced into the liquefied gas supply pump 30 can be eliminated. Of course, as the low-pressure evaporative gas compressor 13 compresses the evaporative gas, the pressure difference that the auxiliary pump 80 solves can be reduced, and furthermore, the low-pressure evaporative gas compressor 13 is supplied to the liquefied gas supply pump 30 The auxiliary pump 80 may be omitted when the evaporation gas is compressed to such an extent as to eliminate the pressure difference between the liquefied gas and the mixed gas. Of course, the low-pressure evaporative gas compressor 13 may be omitted by using the auxiliary pump 80 as an alternative.

Thus, the auxiliary pump 80 is discharged from the in-line mixer 70 by a pressure lowered by mixing with the evaporative gas while the liquefied gas discharged from the liquefied gas storage tank 10 passes through the inline mixer 70 So that the liquefied gas (mixed gas) can be pressurized and delivered to the liquefied gas supply pump 30.

A mixed gas pressure sensor 721 may be provided in the mixed gas supply line 72 for the operation of the auxiliary pump 80 and an auxiliary pump 80 may be provided in accordance with the measured value of the mixed gas pressure sensor 721 The operation can be controlled. The flow rate and temperature of the evaporation gas, the flow rate and temperature of the liquefied gas flowing into the inline mixer 70 may be utilized for the operation of the auxiliary pump 80.

A mixed gas supply valve 722 is provided in the mixed gas supply line 72 and a mixed gas supply valve 722 is provided in the same or similar manner as the auxiliary pump 80 to the liquefied gas branch line 71 The operation can be controlled by the flow sensor 712 or the like.

Unlike the suction drum 20, the in-line mixer 70 of this embodiment is not configured to store the liquefied gas at a predetermined level. Therefore, the in-line mixer 70 of the in- It is necessary to provide means for preventing the problem.

To this end, the auxiliary pump 80 and / or the liquefied gas supply pump 30 may have a suction pot (not shown). The suction pot means a structure in which a space where the mixed gas (or liquefied gas) flowing into the auxiliary pump 80 or the liquefied gas supply pump 30 is temporarily stored, and the auxiliary pump 80 or the like The mixed gas is provided in a locked state in which the liquid is stored, so that only the liquid mixed gas can be sucked up.

Therefore, even if the suction drum 20 is not provided, the present embodiment can prevent the gaseous state from being introduced into the auxiliary pump 80 and the liquefied gas supply pump 30 to sufficiently protect the liquefied gas supply pump 30 and the like have.

The present embodiment further includes a vapor bypass line 14 connected to the consumer 60 bypassing the vaporizer 40 in the liquefied gas storage tank 10 and a high pressure And may further include an evaporative gas compressor 141.

The evaporation gas bypass line 14 is provided so that the evaporation gas discharged from the liquefied gas storage tank 10 is supplied to the consumer 60 without passing through the inline mixer 70, the liquefied gas supply pump 30 and the vaporizer 40 And the inline mixer 70 is provided not to temporarily store the evaporation gas like the suction drum 20 but to prepare for the case where excessive evaporation gas is generated in the liquefied gas storage tank 10 . At this time, unlike the low-pressure evaporative gas compressor 13, the high-pressure evaporative gas compressor 141 can compress the evaporative gas up to the required pressure of the consumer 60 and deliver it to the consumer 60.

As described above, according to the present embodiment, since the suction drum 20 is replaced with the inline mixer 70, the evaporation gas condensation, which is the role of the suction drum 20, and the protection of the liquefied gas supply pump 30 The attraction of the suction drum 20 can be easily secured by omitting the suction drum 20 having a high height and the equipment used for controlling the suction drum 20 need not be provided, have.

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

5, a liquefied gas regeneration system 1 according to a third embodiment of the present invention includes a liquefied gas storage tank 10, a liquefied gas supply pump 30, a vaporizer 40, a fruit supply unit 50 ) And the like, and the fruit supply part 50 may include a fruit recovery line.

The heat recovery line can regulate the pressure of the expansion drum 53 by recovering the heat to the expansion drum 53 at the upstream and downstream sides of the heat heater 52. Specifically, the heat recovery line includes a low temperature heat recovery line 511 for recovering the low temperature heat between the heat pump 51 and the heat insulation heater 52 to the expansion drum 53 and lowering the pressure of the expansion drum 53 can do.

The low temperature heat recovery line 511 recovers the low temperature low temperature heat before being heated by the heat heater 52 after being pressurized by the heat pump 51 to the expansion drum 53. Since the internal temperature of the expansion drum 53 is kept lower than the normal temperature during the normal operation, the pressure may continuously increase due to heat input from the outside. In this case, the low temperature heat recovery line 511 can recover the low temperature heat into the expansion drum 53 in order to prevent overpressure of the expansion drum 53. Since the low temperature heat recovered at this time is in the sub-cooled liquid state, It is possible to reduce the internal pressure of the expansion drum 53 by cooling and condensing the gaseous phase present in the gaseous phase 53.

The low temperature heat recovery valve 511 may be provided with a low temperature heat recovery valve 512 for regulating the recovery flow rate of the low temperature heat and the low temperature heat recovery valve 512 may include a drum pressure sensor 531 The opening degree can be adjusted in accordance with the measured value.

The recovery in the low temperature fruit recovery line 511 may be controlled by a fruit circulation valve 542 provided in the fruit circulation line 54 to control the circulation flow rate of the fruit. The fruit circulation valve 542 can be provided downstream of the point where the low temperature heat recovery line 511 branches from the heat transfer circulation line 54 between the heat pump 51 and the heat heater 52, At least a part of the fruits may be transferred to the low temperature heat recovery line 511 without being transferred to the heat heater 52.

The low temperature heat recovery valve 512 and / or the heat recovery circuit 542 can be controlled by the internal pressure of the expansion drum 53 and / or controlled by the temperature of the heat discharged from the vaporizer 40 have. That is, the recovery by the low-temperature-heat-recovery line 511 is performed in accordance with the measured values of the heat-temperature sensor 541 provided in the drum pressure sensor 531 and / or the heat-recovery circulation line 54 provided in the expansion drum 53 It can be different.

Therefore, the heat circulation valve 542 or the like realizes a function of lowering the internal pressure of the expansion drum 53, while controlling the flow rate of the heat flowing into the vaporizer 40, Can be controlled to be within a predetermined temperature range. Specifically, in this embodiment, the vapor discharged from the vaporizer 40 may be discharged in a sub-cooled liquid state.

The heat recovery line further includes a high temperature heat recovery line (527) in addition to the low temperature heat recovery line (511). The high temperature heat recovery line 527 can recover the high temperature heat between the heating heater 52 and the vaporizer 40 to the expansion drum 53 to increase the pressure of the expansion drum 53. [

The high temperature heat recovery line 527 recovers the high temperature high temperature heat heated by the heat source in the heat heater 52 to the expansion drum 53 and the recovery of the high temperature heat is performed by the expansion drum 53) is excessively lowered, it is possible to raise the internal pressure of the expansion drum (53).

The high temperature heat recovery valve 528 may be provided with a drum pressure sensor 531 provided in the expansion drum 53. The high temperature heat recovery valve 528 may be provided with a high temperature heat recovery valve 528 for regulating the recovery flow rate of the high temperature heat, The opening degree can be controlled according to the measured value.

Therefore, in the present embodiment, the heat transfer valve 542 and / or the low temperature heat recovery valve 512 recover the low temperature heat to the expansion drum 53 so that the temperature of the heat discharged from the vaporizer 40 can be a predetermined temperature However, in this process, the pressure of the expansion drum 53 is continuously lowered. In order to prevent the pressure of the expansion drum 53 from becoming too low, the high-temperature heat recovery valve 528 is operated to recover the high- Can be implemented.

As described above, in the present embodiment, when the fruit such as propane using latent heat is used, the pressure of the expansion drum 53 is effectively controlled to adjust the effective suction head NPSHr of the heat pump 51, The logarithmic mean temperature difference (LMTD) and the heat exchange efficiency at the heater 52 can be increased to reduce the size and price of the vaporizer 40 and the circulation flow rate on the heat transfer line 54 So that the size of the heat transfer line 54 can be reduced.

6 is a conceptual diagram of a liquefied gas regeneration system according to a fourth embodiment of the present invention.

Referring to Figure 6, a liquefied gas regeneration system 1 according to a fourth embodiment of the present invention includes a liquefied gas storage tank 10, a liquefied gas supply pump 30, a vaporizer 40, ), And the like, and the fruit supplying part 50 may include a fruit storage tank 55 and related configurations.

The fruit storage tank (55) stores the fruit discharged from the expansion drum (53). The fruit storage tank 55 may be provided outside the fruit circulation line 54 to maintain the flow rate of the fruit circulating in the fruit circulation line 54 at a certain level.

The expansion drum 53 can continuously absorb the cold heat transferred from the liquefied gas into the space where the continuous circulation of the fruit is performed. However, since the fruit storage tank 55 may not be configured to continuously circulate the fruit during regasification of the liquefied gas, there is a fear that evaporation gas may be generated inside due to external heat penetration.

In the normal temperature range, the fruit storage tank 55 is filled with the fruit storage tank 55 while the temperature rise due to the heat penetration, the generation of the evaporation gas, the increase in the internal pressure of the fruit storage tank 55, Lt; / RTI > may be placed in a state that is no longer subjected to heat penetration.

However, if the ambient temperature rises above the normal level, the supersaturated pressure at ambient temperature may exceed the design pressure of the fruit storage tank 55, and in this case the fruit storage tank 55 may be heated Therefore, problems such as waste of fruit, environmental pollution, and safety threat may occur.

The present embodiment may include a fruit discharge line 554 connected to the upstream of the vaporizer 40 in the fruit circulation line 54 from the fruit storage tank 55 to solve this problem. The fruit discharge line 554 can transfer the vapor in the vapor phase to the vaporizer 40 when heat is generated in the fruit storage tank 55 and the vapor in the fruit storage tank 55 is generated.

Thus, in the present embodiment, when overpressure is generated in the fruit storage tank 55, the vapor is discharged to the outside of the fruit storage tank 55, and the fruit is not discharged to the outside of the fruit supply part 50, can do.

Specifically, the gaseous effluent discharged through the fruit discharge line 554 can be recovered after liquefied by the liquefied gas in the vaporizer 40, the liquefied fruit is recovered to the expansion drum 53, 54 or may be conveyed back to the fruit storage tank 55.

A fruit branch line 551 may be provided from the expansion drum 53 to the fruit storage tank 55 so that the fruit can be transferred from the expansion drum 53 to the fruit storage tank 55. [ The fruit branching line 551 may be provided with a fruit branching pump 552 and the fruit branching pump 552 may transfer the liquid fruit stored in the expansion drum 53 to the fruit storage tank 55.

The expansion drum 53 may be provided with a drum level sensor 532 for measuring the level of the fruit stored in the expansion drum 53. When the level in the expansion drum 53 is too high, The liquid fruit can be transferred from the liquid storage tank 53 to the fruit storage tank 55. Thus, the flow rate of the fruit circulating along the fruit circulation line 54 is adjusted to a non-excessive and stable level. Of course, the heat branch pump 552 may be controlled to operate based on the internal pressure of the expansion drum 53, in addition to the level in the expansion drum 53. [

The liquid-state fruit introduced into the fruit storage tank 55 is stored in the fruit storage tank 55 without being circulated in the regeneration process of the liquefied gas, and can be vaporized into the vapor in the vapor phase by external heat penetration, The inner pressure of the fruit storage tank 55 is increased.

However, as described above, the internal temperature of the fruit storage tank 55 may converge to the outside air temperature and the internal pressure may be a pressure that the fruit is placed in a supersaturated state. In the region where the vessel having the fruit storage tank 55 is located The meteorological fruit generated in the fruit storage tank 55 is supplied to the fruit storage tank 554 through the fruit discharge line 554 in consideration of the supersaturated pressure exceeding the design pressure of the fruit storage tank 55 55, respectively. As a result, the present embodiment can reduce the design pressure of the fruit storage tank 55 and prevent over designing of the fruit storage tank 55.

The fruit storage tank 55 can store the fruit at a relatively higher pressure than the expansion drum 53. [ This is because, in the case of the fruit storage tank 55, the continuous circulation of the fruit does not occur, so that the internal pressure of the fruit storage tank 55 rises while the fruit is vaporized due to external heat penetration.

For example, if the internal pressure of the suction drum 20 is in the range of about 0.1 to 2 bar (for example, 0.5 bar), the internal pressure of the fruit storage tank 55 may be about 2 to 10 bar (for example, 4 bar). Way branch line 551 may be provided with a one way valve 5511 for limiting the flow of the heat in one direction so that the flow of the heat does not flow from the heat storage tank 55 to the suction drum 20. [

Also, the fruit storage tank 55 can store the fruit at a pressure relatively higher than the pressure of the fruit flowing in the vaporizer 40. For example, the pressure of the fruit flowing in the vaporizer 40 may be about 1 to 5 bar (for example, 2 bar), and the internal pressure of the fruit storage tank 55 may be about 2 to 10 bar (4 bar for example) higher. In this case, a one-way valve 5541 for limiting the flow of the heat in one direction may be provided in the heat discharge line 554.

The present embodiment may be provided with a tank pressure sensor 553 for measuring the pressure of the fruit storage tank 55 and the tank pressure sensor 553 may be provided on the fruit storage tank 55 itself or on the fruit discharge line 554 As shown in FIG.

The fruit discharge line 554 may be provided with a fruit discharge valve 555 which discharges the flow rate of the fruit discharged from the fruit storage tank 55 according to the measured value of the tank pressure sensor 553 Can be adjusted.

Therefore, the fruit storage tank 55 can have an internal pressure in which the fruit is placed in a supersaturated state when the temperature of the surrounding region is ordinary, and when the temperature in the surrounding region is very high, the internal pressure The vapor of the vapor phase is discharged to the vaporizer 40 through the fruit discharge line 554 to ensure structural stability.

Thus, in order to solve the problem that the internal pressure of the fruit storage tank 55 storing the fruit is excessively increased due to infiltration of the external heat, the present embodiment is characterized in that the vapor of the vapor generated in the fruit storage tank 55 is supplied to the vaporizer 40 and liquefied and reused, the durability of the fruit storage tank 55 can be maintained even if the design pressure of the fruit storage tank 55 is lowered.

It is needless to say that the present invention is not limited to the above-described embodiments, and that a combination of the above embodiments or a combination of at least any of the above-described embodiments with known techniques can be included as another embodiment.

While the present invention has been particularly shown and described with reference to exemplary embodiments thereof, it is to be understood that the invention is not limited to the disclosed embodiments, but, on the contrary, It will be apparent to those skilled in the art that various combinations and modifications may be made without departing from the scope of the present invention. Therefore, it should be understood that the technical contents related to the modifications and applications that can be easily derived from the embodiments of the present invention are included in the present invention.

1: liquefied gas regeneration system 10: liquefied gas storage tank
11: Transfer pump 12: Liquefied gas supply line
13: Evaporative gas supply line 14: Evaporative gas bypass line
20: Suction drum 21:
22: liquefied gas discharge line 30: liquefied gas supply pump
31: liquefied gas return line 40: vaporizer
50: fruit supply part 51: fruit pump
52: Fruit heater 53: Expansion drum
54: fruit circulation line 55: fruit storage tank
60: Demand 70: Inline Mixer
71: liquefied gas branch line 72: mixed gas supply line
80: auxiliary pump

Claims (8)

A liquefied gas supply pump for pressurizing the liquefied gas discharged from the liquefied gas storage tank;
A vaporizer for vaporizing the pressurized liquefied gas by the liquefied gas supply pump and supplying it to a customer;
An inline mixer for mixing the vaporized gas and the liquefied gas discharged from the liquefied gas storage tank and delivering the liquefied gas to the liquefied gas supply pump; And
A mixer for mixing the liquefied gas supplied from the in-line mixer with the liquefied gas supplied from the in-line mixer to the liquefied gas supply pump; Further comprising an auxiliary pump for compensating for the temperature of the liquefied gas. The in-line mixer according to claim 1,
And a suction drum provided between the liquefied gas storage tank and the liquefied gas supply pump. The method according to claim 1,
An evaporation gas supply line connected to the in-line mixer in the liquefied gas storage tank;
A liquefied gas supply line connected from the liquefied gas storage tank to the customer via the liquefied gas supply pump;
A liquefied gas branch line branched from the liquefied gas supply line upstream from the liquefied gas supply pump and connected to the inline mixer; And
And a mixed gas supply line connected to the liquefied gas supply line or the liquefied gas supply pump through the auxiliary pump in the inline mixer. The method of claim 3,
Further comprising a low-pressure evaporative gas compressor provided on the evaporative gas supply line. 5. The method of claim 4,
A vapor bypass line connected to the consumer by bypassing the vaporizer in the liquefied gas storage tank; And
Further comprising a high pressure evaporative gas compressor provided on the evaporative gas bypass line. 4. The pump according to claim 3,
And the liquefied gas discharged from the liquefied gas storage tank is passed through the inline mixer to pressurize the liquefied gas discharged from the inline mixer to the liquefied gas supply pump by a pressure lowered by mixing with the evaporation gas The liquefied gas regeneration system comprising: The method of claim 3,
Further comprising a mixed gas pressure sensor provided in the mixed gas supply line,
Wherein the auxiliary pump is operated in accordance with a measured value of the mixed gas pressure sensor. A ship having the liquefied gas regeneration system of any one of claims 1 to 7.

Images