KR101792410B1 - Regasification System of liquefied Gas and Ship Having the Same - Google Patents

Abstract

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a liquefied gas regeneration system and a ship having the liquefied gas regeneration system, including a liquefied gas storage tank for storing liquefied gas; A main line connected to the customer from the liquefied gas storage tank; A vaporizer provided in the main line for vaporizing the liquefied gas; A bypass line branching from the main line; A liquefied gas drum provided on the main line or the bypass line for temporarily storing the liquefied gas; And a mixer provided upstream of the liquefied gas drum in the main line or the bypass line and mixing the evaporated gas in the liquefied gas storage tank with the liquefied gas.

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 in order to solve the problems of the prior art as described above, and it is an object of the present invention to provide a liquefied gas storage tank in which evaporation gas is mixed with liquefied gas upstream of a liquefied gas drum, So that the evaporated gas can be utilized.

A liquefied gas regeneration system according to an aspect of the present invention includes a liquefied gas storage tank for storing a liquefied gas; A main line connected to the customer from the liquefied gas storage tank; A vaporizer provided in the main line for vaporizing the liquefied gas; A bypass line branching from the main line; A liquefied gas drum provided on the main line or the bypass line for temporarily storing the liquefied gas; And a mixer provided upstream of the liquefied gas drum in the main line or the bypass line and mixing the evaporated gas in the liquefied gas storage tank with the liquefied gas.

Specifically, the mixer can condense at least a part of the evaporated gas using the liquefied gas and supply it to the liquefied gas drum.

Specifically, the evaporator may further include an evaporation gas supply line connected to the mixer in the liquefied gas storage tank to deliver the evaporated gas in the liquefied gas storage tank.

Specifically, the evaporation gas supply line may be branched upstream of the mixer and connected to the liquefied gas drum.

The main line and the evaporation gas supply line may further include a heat exchanger that flows through the main line and the evaporation gas supply line and cools the evaporation gas into liquefied gas. The evaporation gas supply line is branched from the upstream of the mixer, Gas drum.

Specifically, it may include at least one evaporative gas valve provided in the evaporative gas supply line and controlling the flow rate of the evaporative gas supplied to the mixer or the liquefied gas drum.

Specifically, the evaporation gas valve may control the flow rate of the evaporation gas supplied to the mixer or the liquefied gas drum based on the flow rate of the evaporation gas generated in the liquefied gas storage tank.

Specifically, the evaporation gas valve opens the evaporation gas supply line connected to the mixer when the flow rate of the evaporation gas generated in the liquefied gas storage tank is less than a preset value, and in the liquefied gas storage tank And the evaporation gas supply line connected to the heat exchanger and the liquefied gas drum can be opened when the flow rate of the generated evaporation gas is equal to or greater than a predetermined value.

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

The liquefied gas regeneration system according to the present invention can mix the vaporized gas with the liquefied gas upstream of the liquefied gas drum to prevent the overpressure of the liquefied gas storage tank and to realize the recycling of the evaporated gas.

1 is a conceptual view of a liquefied gas regeneration system according to a first embodiment of the present invention;
2 is a conceptual diagram of a liquefied gas regeneration system according to a second embodiment of the present invention;
3 is a conceptual diagram of a liquefied gas regeneration system according to a third embodiment of the present invention.
4 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.

Hereinafter, the liquefied gas may be used in terms of a liquid state, a natural vaporized state, or a forced vaporized gas state, but the term "vaporized gas" refers to a gas that is spontaneously vaporized in the liquefied gas storage tank 10 As shown in FIG.

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. Hereinafter, the liquefied gas regeneration system 1 of the present invention will be described, and the present invention includes a liquefied gas regeneration system 1 and a vessel having the same.

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

1, a liquefied gas regeneration system 1 according to a first embodiment of the present invention includes a liquefied gas storage tank 10, a liquefied gas pump 30, a vaporizer 40, a liquefied gas drum 20 ).

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 100.

The liquefied gas in the liquefied gas storage tank 10 can be maintained in a liquid state, but can be spontaneously vaporized into an evaporated gas due to various factors such as external heat penetration. At this time, the evaporated gas may be transferred to the liquefied gas drum 20 through an evaporative gas compressor 23a to be described later.

The liquefied gas pump (30) delivers the liquefied gas to the vaporizer (40). The liquefied gas pump 30 may be provided inside and / or outside the liquefied gas storage tank 10 and can pressurize the liquefied gas stored in the liquefied gas storage tank 10 and deliver it to the vaporizer 40 .

At this time, the liquefied gas pump 30 may pressurize the liquefied gas of 1 to 5 bar to the vaporizer 40 within 60 bar. Of course, the pressure of the liquefied gas discharged from the liquefied gas pump 30 can be variously determined according to the required pressure of the consumer 100.

A plurality of liquefied gas pumps 30 may be provided, one of which may be a main and the other may be an auxiliary, and a plurality of liquefied gas pumps 30 may be provided in parallel. Further, the liquefied gas pump 30 may be provided with a primary pump and a secondary pump. The primary pump and the secondary pump are provided in series with each other. The secondary pump adds liquefied gas pressurized by the primary pump Lt; / RTI >

The vaporizer (40) vaporizes the liquefied gas. The customer 100 supplied with the vaporized liquefied gas may be an engine or a turbine that produces energy or may be an end consumer such as a city gas or a general household. In the customer 100, a liquefied gas is vaporized by the vaporizer 40 Lt; / RTI >

The main line 11 for supplying the liquefied gas can be connected from the liquefied gas storage tank 10 to the consumer 100 via the liquefied gas pump 30 and the vaporizer 40. Various valves (not shown) are provided in the main line 11 to control the supply flow rate of the liquefied gas, and a bypass line 12 to be described later can be branched.

The vaporizer 40 can heat the liquefied gas using various fruits. For example, the present embodiment can heat the liquefied gas using the glycol water without the risk of corrosion of heat exchangers, pipes, and the like. Glycol water is not explosive, safe, cheap and easy to change composition.

For this purpose, the vaporizer 40 may be provided with a structure for supplying the heat. The structure for supplying the heat may include a heat source line 41, a heat source heater 42, a heat pump 43, and the like.

The fruit line (41) is connected to the vaporizer (40) and supplies the fruit to the vaporizer (40). The fruit line 41 may be provided in a closed loophal form so that the fruit delivered to the vaporizer 40 can be circulated by the fruit line 41.

On the fruit line 41, a fruit heater 42 and a fruit pump 43 may be provided. The fruit heater 42 can heat the cooled fruit while exchanging heat with the liquefied gas. At this time, although the present embodiment uses seawater, it is needless to say that various heat such as steam, heat generated by electricity, engine exhaust, heat of engine cooling water, and waste heat generated by ship can be used. Hereinafter, for convenience, the present embodiment is limited to heating fruits using seawater.

The fruit heater (42) heats the fruit using seawater. The fruit heater 42 may be a heat exchanger similar to the vaporizer 40 and may transfer heat contained in the seawater to the fruit to heat the fruit.

The fruit pump 43 transfers the heated fruit to the vaporizer 40. The fruit pump 43 may be provided for flow of the fruit, and the fruit may be pressurized to increase the heat exchange efficiency.

The heat pump 43 may be provided in parallel as described for the liquefied gas pump 30, at least one of which may be used as the main and the other as auxiliary.

A fruit temperature sensor 46 may be provided upstream or downstream of the vaporizer 40 (specifically between the fruit heater 42 and the fruit pump 43). The fruit-temperature sensor 46 measures the temperature of the fruit heated by the fruit-heater 42 and determines whether the temperature of the fruit is sufficiently elevated (when the fruit is cooled by the liquefied gas, Or whether it is too much (whether the water contained in the fruit glycol glycol is vaporized and cracked, or whether cracking occurs).

The flow rate of the seawater for supplying heat to the fruit in relation to the fruit in the fruit heater 42 can be varied according to the temperature of the fruit sensed by the fruit temperature sensor 46. [ A heating line 42a for supplying seawater may be connected to the fruit heater 42 and a seawater pump 42b may be provided for the heating line 42a. May be transmitted to a valve (not shown) provided in the seawater pump 42b and / or the heating line 42a to vary the flow rate of seawater.

That is, if the temperature of the fruit is measured to be too low, the flow rate of the seawater can be increased to heat the fruit sufficiently. On the contrary, if the temperature of the fruit is measured too high, the flow rate of the seawater can be reduced to have a proper temperature. Thus, the present embodiment can maintain the temperature of the fruit in a stable state in which freezing or vaporization is prevented.

This embodiment is not shown in the drawing, but a line (not shown) that bypasses the heater 42 in the fruit line 41 can be additionally provided and the flow rate of the fruit flowing in the bypass line is controlled The temperature of the fruit can also be adjusted.

An additional heater 47 may be provided downstream of the fruit heater 42. The additional heater 47 can further heat the fruit based on the temperature of the fruit sensed by the fruit temperature sensor 46. The additional heater 47 provides the load of the fruit pump 43 Can be saved.

When the viscosity of the fruit is high, the flow of the fruit becomes difficult and the load of the fruit pump 43 may be increased. have. On the other hand, when the viscosity of the fruit is low, the flow of the fruit is facilitated and the load of the fruit pump 43 can be reduced.

However, the viscosity of the fruit varies depending on the temperature of the fruit. If the temperature of the fruit is high, the viscosity can be lowered. If the temperature of the fruit is low, the viscosity can be increased. That is, the temperature of the fruit detected by the fruit temperature sensor 46 may be a value indirectly representing the viscosity of the fruit.

At this time, the additional heater 47 can calculate the viscosity of the fruit based on the temperature of the fruit, and further heat the fruit to lower the viscosity of the fruit. The additional heater 47 lowers the viscosity of the fruit by heating the fruit on the basis of the load of the heat pump 43 so that the load of the heat pump 43 is lowered It can be kept below the reference value. Therefore, power consumption can be reduced.

Of course, even if the additional heater 47 further heats the fruit, it can be done within a range in which vaporization of the fruit is prevented. Therefore, in this embodiment, the vaporization prevention value, which is the temperature for preventing the vaporization of the heat, is set, and the operation of the additional heater 47 can be performed within a range not exceeding the vaporization prevention value.

As described above, the additional heater 47 can further heat the fruit on the basis of the load of the heat pump 43 calculated or predicted according to the temperature of the fruit, and the viscosity of the fruit is controlled by the additional heater 47, The additional heater 47 may be provided upstream of the heat pump 43 so that the load of the pump 43 is lowered.

The fruit line (41) may be provided with a fruit control part (44). The fruit regulation part (44) regulates the composition of the fruit flowing in the fruit line (41). The fruit is composed of a mixture of at least two different substances, for example, a glycol water which is a mixture of ethylene glycol and water as described above. When the fruit is cooled in the vaporizer 40 by the liquefied gas, Water may freeze.

At this time, the risk of freezing of the fruit may vary depending on the ratio of the water mixed with the fruit. If the fruit is mixed with water, the risk of freezing of the fruit is inevitably increased. Therefore, in this embodiment, by controlling the ratio of the substance contained in the fruit by using the fruit controlling part 44, it is possible to prevent the freezing of the fruit.

That is, the fruit regulator 44 can vary the freezing point of the fruit by controlling the ratio of ethylene glycol and / or water contained in the fruit based on the temperature of the fruit sensed by the fruit temperature sensor 46. [ That is, if the specific gravity of ethylene glycol in the fruit is increased or the specific gravity of water is lowered by the fruit control part 44, the freezing point of the fruit will be lowered, so that the freezing of the fruit can be prevented.

The fruit controlling part 44 can control the ratio of ethylene glycol (glycol) contained in the fruit, and when the temperature of the fruit is less than the predetermined value, the freezing point of the fruit can be lowered by increasing the ratio of the glycol. However, if the ratio of the glycol to the fruit increases, the viscosity of the fruit increases, and the load of the fruit pump 43 rises or the flow velocity decreases, and the possibility of freezing may occur. Therefore, the fruit regulator 44 can increase the ratio of the glycol within the limit of the fluidity of the fruit being equal to or higher than the predetermined value (the viscosity of the fruit is below the reference value).

That is, in this embodiment, the load of the fruit pump 43 can be reduced by further heating the fruit so that the viscosity of the fruit is lowered, while the proportion of the glycol can be increased so that the freezing point of the fruit is lowered. However, in the latter case, as the ratio of glycol increases, the viscosity of the fruit increases, and further heating by the additional heater 47 may occur. In other words, the operation of the additional heater 47 can be linked to the adjustment of the component of the fruit by the fruit adjusting part 44.

A pressure regulating tank 44 may be provided in the fruit line 41 in place of the fruit regulating section 44 or the fruit regulating section 44 described above. The pressure regulating tank 44 and the fruit regulating portion 44 are shown as one configuration in the figure and if the pressure regulating tank 44 is filled with glycol, the pressure regulating tank 44 can be used as the heat regulating portion 44 It is because. It is to be understood that the present embodiment may be provided with the pressure regulating tank 44 and the heat regulating unit 44 separately, but it is assumed that there is only one heat regulating unit 44 and one pressure regulating tank 44 do.

The pressure regulating tank 44 may temporarily store the fruit (or glycol). At this time, the pressure regulating tank 44 can further supply the fruit (glyco) to the fruit line 41 to increase the pressure of the fruit flowing in the fruit line 41. To this end, the pressure regulating tank 44 may be provided with a pressure regulating line 45. The pressure regulating line 45 is provided with an injection valve 45a and a discharge valve 45b and is used for injecting a fuel or a pressure regulating gas (an inert gas such as nitrogen) into the pressure regulating tank 44, 44 or the pressure regulating gas.

The injection valve 45a is opened when the pressure of the fruit is lower than the reference value and the pressure of the fruit in the fruit line 41 is increased as the fruit or the like is supplied to the pressure regulating tank 44. On the contrary, 45b are opened when the pressure of the fruit becomes higher than the reference value so that the heat is discharged from the pressure regulating tank 44 to the outside so that the pressure of the fruit in the fruit line 41 is lowered.

This series of control changes the pressure of the liquor in the liquor line 41, which can be brought together in conjunction with control to further heat the liquor or to control the ingredient ratio in the liquor.

Together with the pressure regulating tank 44 or separately, the pressure of the fruit can be regulated by the fruit pump 43. In other words, since the pressure of the fruit is also adjustable in the fruit pump 43, the fruit pump 43 can increase the pressure of the fruit discharged from the fruit pump 43 by raising the load RPM based on the temperature of the fruit.

A high-pressure gas injection unit 48 may be provided in the fruit line 41. The high-pressure gas injection unit 48 is capable of injecting high-pressure gas into the fruit line 41 when the operation of the fruit pump 43 is less than a predetermined value or is stopped, that is, when the flow of the fruit is lower than the preset speed . The operation of the fruit pump 43 may be grasped on the basis of the rotational speed RPM as a load of the fruit pump 43 and the high pressure gas injecting part 48 may be grasped on the fruit pump 43 This is to prepare for when the problem occurs and the flow of the fruit is slowed down.

The high-pressure gas injection unit 48 can prevent freezing of the fruit. In other words, the high-pressure gas injection unit 48 blows the high-pressure gas to the fruit line 41 to thereby increase the flow rate of the fruit in the fruit line 41 so that the fruit can not be frozen.

In other words, the high-pressure gas injecting section 48 can blow the inert gas such as nitrogen into the high-pressure gas line 41 by increasing the flow rate of the heat to prevent freezing of the heat, (40). This is to prevent the freezing of the fruit in the vaporizer 40 when it is cooled.

Specifically, the high-pressure gas injection unit 48 can be connected between the heat pump 43 and the vaporizer 40 or between the vaporizer 40 and the heater heater 42. The high-pressure gas is introduced into the vaporizer 40, It is possible to accelerate the flow of the heat in the heat exchanger 40, thereby preventing the freezing of the fruit.

However, when the high-pressure gas is injected, the liquefied gas may not be vaporized properly due to failure of the heat pump 43. Therefore, when the high-pressure gas injection unit 48 is operated, (Liquefied gas storage tank 10 or the like), at least a part of it may be returned to the demanding place 100 through the return line (Not shown) provided in the return line may be adjusted in accordance with an operation signal of the high-pressure gas injection unit 48. [

When the high-pressure gas is injected into the fruit line 41, the fruit can be pushed out by the high-pressure gas. At this time, the present embodiment can keep the fruit line 41 closed and increase the pressure of the fruit in the fruit line 41 by the addition of the high-pressure gas, or the fruit pushed out by the high- And a fruit regulating part 44 for allowing the fruit to flow out and stored. The fruit adjusting part 44 may be a pressure adjusting tank 44 or the like as described above.

The liquefied gas drum 20 is provided between the liquefied gas storage tank 10 and the vaporizer 40 and may be provided on the bypass line 12 in detail. The bypass line 12 may be provided to branch off from the main line 11 and to join the main line 11 upstream of the liquefied gas pump 30 and to control the flow rate of the liquefied gas May be provided.

Bypass line 12 is a line that bypasses some of the liquefied gas from main line 11, such as a term expression. The liquefied gas discharged from the liquefied gas storage tank 10 and directed toward the vaporizer 40 may flow primarily through the main line 11 and may not flow or flow supplementally through the bypass line 12. [

To this end, the main line 11 may have a relatively large flow rate of the liquefied gas relative to the bypass line 12, wherein the specification refers to the diameter of the line, Resistance and the like.

The liquefied gas drum 20 may temporarily store some of the liquefied gas delivered through the bypass line 12, rather than most of the liquefied gas delivered to the main line 11. The liquefied gas drum 20 temporarily stores the liquefied gas and delivers the liquefied gas to the liquefied gas pump 30 so that the liquefied gas pump 30 can be stably driven.

The internal pressure of the liquefied gas drum 20 can be maintained at an appropriate level and can be maintained at a relatively high pressure relative to the internal pressure of the main line 11. [ The liquefied gas drum 20 may be a gas-liquid separator for separating the liquefied gas delivered through the bypass line 12 into a liquid component and a gaseous component and delivers the liquid component to the main line 11 to be supplied to the liquefied gas pump 30 .

The liquefied gas drum 20 may be provided with a minimum flow line 31. In order to protect the liquefied gas pump 30, the liquefied gas pump 30 must continuously flow with a minimum amount of liquefied gas. To this end, the inside or the outlet of the liquefied gas pump 30 or the liquefied gas pump 30 The minimum flow line 31 can be connected to the liquefied gas drum 20.

The minimum flow line 31 may be connected to the intermediate point on the liquefied gas drum 20 in the vertical direction and the point where the minimum flow line 31 is connected may be connected to the level of the liquefied gas held in the liquefied gas drum 20 May be a higher point. This is because the liquefied gas returned through the minimum flow rate line 31 is in a liquid phase, so that it is sprayed on the gas component in the liquefied gas drum 20 to realize liquefaction of the gas component.

The minimum flow rate line 31 is connected to the liquefied gas drum 20 in the liquefied gas pump 30 but can be connected to the liquefied gas pump 30 in such a way that liquefied gas in an unpressurized state or liquefied gas in a less- have. In other words, the minimum flow rate line 31 can be branched at the point before the pressurization in the liquefied gas pump 30 and connected to the liquefied gas drum 20.

The liquefied gas drum 20 may be provided with a heating line (not shown) for heating the liquid liquefied gas stored therein and returning the liquefied gas to the liquefied gas drum 20. A heater (not shown) May be provided. That is, the inside of the liquefied gas drum 20 can be boosted while heating the liquefied gas in the liquefied gas drum 20 and returning it to the liquefied gas drum 20, The transfer of the liquefied gas can be performed naturally without a separate press-feeding structure.

The minimum flow rate line 31 is that the liquefied gas before it is completely pressurized by the liquefied gas pump 30 is transferred to the liquefied gas drum 20 and is able to liquefy the evaporated gas in the liquefied gas drum 20, (20) can be realized.

An evaporation gas supply line (23) may be connected to the liquefied gas drum (20). The evaporation gas supply line 23 can supply the evaporation gas generated in the liquefied gas storage tank 10 to the liquefied gas drum 20, and the evaporation gas compressor 23a can be provided.

The evaporation gas flows along the evaporation gas supply line 23 and is compressed by the evaporation gas compressor 23a and then supplied to the liquefied gas drum 20. In this case, The pressure inside the liquefied gas drum 20 can be increased as the liquefied gas is introduced into the liquefied gas drum 20.

That is, the pressure in the liquefied gas drum 20 can be controlled by the liquefied gas or the evaporative gas supplied through the minimum flow line 31, the evaporation gas supply line 23, through which the liquefied gas drum 20 It is possible to maintain the internal pressure at a relatively high pressure relative to the main line 11.

A pressure regulating line 22 may be connected to the liquefied gas drum 20. The pressure regulating line 22 may be provided with an injection valve 22a and a discharge valve 22b. The pressure regulating line 22 is a constitution in which an inert gas such as nitrogen or a pressure regulating gas such as a liquefied gas or an evaporating gas is injected into the liquefied gas drum 20 or taken out from the liquefied gas drum 20, The injection of the regulating gas is performed by the injection valve 22a and the discharge of the pressure regulating gas by the discharge valve 22b.

That is, the pressure regulating line 22 can increase the internal pressure of the liquefied gas drum 20 through the injection of the pressure regulating gas or lower the internal pressure of the liquefied gas drum 20 through the discharge of the pressure regulating gas. At this time, the evaporation gas supply line 23 may be connected to the liquefied gas drum 20 through the pressure regulating line 22.

The injection valve 22a is opened when the pressure of the liquefied gas drum 20 reaches the lower limit value, so that the pressure regulating gas can be introduced into the liquefied gas drum 20. [ On the other hand, the discharge valve 22b is opened when the pressure of the liquefied gas drum 20 reaches the upper limit value, so that the pressure regulating gas can be discharged from the liquefied gas drum 20. [ Therefore, the present embodiment can keep the internal pressure of the liquefied gas drum 20 constant at an appropriate level.

However, if there is an evaporative gas in the liquefied gas drum 20 in the course of discharging the pressure-regulating gas, the evaporated gas can also escape to the pressure regulating line 22 through the discharge valve 22b. Therefore, in this embodiment, a temperature sensor (not shown) for sensing the temperature in the liquefied gas drum 20 is provided so that only the gas for regulating the pressure such as inert gas is discharged by the discharge valve 22b, It is possible to prevent the discharge valve 22b from being used or to prevent the evaporation gas from escaping to the pressure regulating line 22 when the temperature inside the evaporator 20 is higher than the reference value.

In this way, the present embodiment can control the pressure of the liquefied gas drum 20 through injection or discharge for regulating pressure. In summary, the internal pressure of the liquefied gas drum 20 is controlled by the evaporation gas supply line 23, Through the injection valve 22a of the pressure regulating line 22 or through the discharge valve 22b of the minimum flow line 31 and the pressure regulating line 22. [

Of course, a pressure sensor (not shown) and a temperature sensor (not shown) may be provided on the liquefied gas drum 20 to maintain the pressure in the liquefied gas drum 20 at a constant level, May be used to adjust the opening of the valves provided in each of the above-described lines.

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

2, 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 pump 30, a vaporizer 40, a liquefied gas drum 20 ), And further includes a heat exchanger (60). Hereinafter, the present embodiment will mainly be described with respect to different points from the above-described other embodiments, and the description omitted is replaced with the description of the other embodiments.

In this embodiment, the liquefied gas drum 20 may be provided in the main line 11 or the bypass line 12 and temporarily store the liquefied gas. At this time, the evaporation gas supply line 23 may be connected to the liquefied gas drum 20, and a spray 20a may be provided inside the liquefied gas drum 20 to spray the liquefied gas.

The spray 20a may be located at the top in the liquefied gas drum 20 and the evaporation gas supply line 23 may be connected at a lower height than the spray 20a. Therefore, the evaporation gas flowing into the liquefied gas drum 20 through the evaporation gas supply line 23 can be condensed by the liquefied gas injected from the spray 20a.

The spray 20a may be provided at one end connected to the liquefied gas drum 20 in the main line 11 or the bypass line 12 and may be provided in the liquefied gas drum 20 in a low- It can be sprayed downward. At this time, the evaporation gas flowing through the evaporation gas supply line 23 can be cooled and condensed at a low temperature while meeting with the liquefied gas sprayed from above.

The evaporation gas supply line 23 can be connected to a level higher than the level of the liquefied gas temporarily stored in the liquefied gas drum 20. The evaporation gas flowing along the evaporation gas supply line 23 can be injected into the upper portion of the liquid liquefied gas stored in the liquefied gas drum 20.

This is to prevent vaporization of the liquefied gas stored in the liquid phase while bubbles are generated when the evaporation gas is injected into the liquid liquefied gas, or the level of the liquefied gas in the liquefied gas drum 20 is shaken and unstable. That is, the present embodiment is characterized in that the evaporation gas supply line 23 is provided at a height higher than the level of the liquefied gas stored therein so that the level of the liquefied gas in the liquefied gas drum 20 is stably maintained and the generation of bubbles is suppressed. Can be introduced.

The spray 20a and the evaporation gas supply line 23 may be sequentially connected from the upper part of the liquefied gas drum 20 to the lower part thereof. However, in the case of the minimum flow line 31 described in the previous embodiment, it may be joined to the main line 11 or the bypass line 12 upstream of the spray 20a.

At this time, the liquefied gas drum 20 can condense the evaporation gas supplied by the evaporation gas supply line 23 by the liquefied gas sprayed by the spray 20a.

The heat exchanger 60 is provided between the liquefied gas pump 30 and the customer 100 and the main line 11 and the evaporation gas supply line 23 are connected to each other. The heat exchanger 60 can cool the evaporation gas flowing along the evaporation gas supply line 23 to the liquefied gas flowing along the main line 11. The heat exchanger 60 may be located upstream of the vaporizer 40 for this purpose.

The heat exchanger (60) may be provided upstream of the liquefied gas drum (20) in the evaporation gas supply line (23). The evaporated gas discharged from the liquefied gas storage tank 10 and flowing along the evaporated gas supply line 23 is first cooled by the liquefied gas in the heat exchanger 60 and then introduced into the liquefied gas drum 20 And can be secondarily cooled and condensed by the liquefied gas injected by the spray 20a.

Therefore, the present embodiment can condense the evaporated gas in the liquefied gas drum 20 and preheat the liquefied gas upstream of the evaporator 40 in the process of primarily cooling the evaporated gas, ) Of the fruit to be used in the heat treatment (the total heat amount according to the flow rate of the fruit and the temperature).

In the present embodiment, as shown in the drawing, the vaporizer 40 can use seawater as a heat source, and a fruit pump 43 (seawater pump) is provided in the fruit line 41 connected to the carburetor 40 . Also, the seawater as the fruit can be heated by steam, and the heating line 42a for heating the fruit may be provided with a boiler 42c for generating steam.

Of course, it is noted that, in this embodiment, the configuration of the supply of the fuel to be connected to the carburetor 40 can be replaced or merged with the configuration described in the other embodiments. This applies equally to the embodiments described below.

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

Referring to FIG. 3, 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 pump 30, a vaporizer 40, and a liquefied gas drum 20, and further includes a mixer 50. Hereinafter, the present embodiment will mainly be described with respect to different points from the above-described other embodiments, and the description omitted is replaced with the description of the other embodiments.

The mixer 50 is provided upstream of the liquefied gas drum 20 in the main line 11 or the bypass line 12 and mixes the evaporated gas in the liquefied gas storage tank 10 into the liquefied gas. The mixer 50 can condense at least a portion of the evaporated gas using the liquefied gas and supply it to the liquefied gas drum 20.

The evaporation gas supply line 23 connected at one end to the liquefied gas storage tank 10 may be connected to the mixer 50 or the heat exchanger 60. That is, the evaporation gas supply line 23 may be branched at a certain point (for example, downstream of the evaporation gas compressor 23a) and connected to the mixer 50, and the compressed evaporation gas may be supplied to the mixer 50.

Accordingly, the mixer 50 can mix the low-pressure liquefied gas and the relatively high-pressure evaporation gas to at least partially condense the evaporated gas and then transfer it to the liquefied gas drum 20. This is because, when the evaporation gas is compressed and then supplied to the mixer 50, the boiling point is increased at the time of compression, which is advantageous for liquefaction.

In addition, the evaporation gas supplied to the mixer 50 may be cooled while being decompressed so as to balance the pressure with the liquefied gas supplied to the mixer 50. That is, the present embodiment can primarily condense the evaporated gas while mixing the high-pressure evaporation gas with the liquid-phase liquefied gas of low pressure and low temperature in the mixer 50.

The evaporation gas flows along the evaporation gas supply line 23 and is branched and mixed with the liquefied gas while being introduced into the mixer 50 and then supplied to the liquefied gas drum 20 after condensation and condensation or is supplied to the heat exchanger 60 Exchanged and cooled and then supplied to the liquefied gas drum 20. At this time, the height supplied to the liquefied gas drum 20 through the mixer 50 may be higher than the height supplied to the liquefied gas drum 20 through the heat exchanger 60.

This is because the evaporated gas flowing through the mixer 50 is more likely to be condensed than the evaporated gas flowing through the heat exchanger 60, so that the evaporated gas condensed through the mixer 50 is sprayed from above, So as to condense the evaporated gas. A spray 20a is provided on the liquefied gas drum 20 so that the liquefied gas and the evaporated gas mixed in the mixer 50 can be sprayed downward through the spray 20a.

The evaporation gas supply line 23 may be provided with at least one evaporation gas valve (not shown) for controlling the flow rate of the evaporation gas supplied to the mixer 50 or the liquefied gas drum 20, as described above have. The evaporation gas valve may be provided downstream and / or upstream of the point where it branches to the mixer 50 and the heat exchanger 60 on the evaporation gas supply line 23 and may occur in the liquefied gas storage tank 10 The flow rate of the evaporating gas supplied to the mixer 50 or the liquefied gas drum 20 can be adjusted based on the flow rate of the evaporating gas.

Specifically, the evaporation gas valve opens the evaporation gas supply line 23 connected to the mixer 50 when the flow rate of the evaporation gas generated in the liquefied gas storage tank 10 is less than a preset value, The evaporation gas supply line 23 connected to the heat exchanger 60 and the liquefied gas drum 20 can be opened when the flow rate of the evaporation gas generated in the evaporator 10 is equal to or greater than a predetermined value.

A temperature sensor (not shown) or a pressure sensor (not shown) may be provided in the liquefied gas storage tank 10 to detect the flow rate of the evaporation gas. The sensed value is transferred to the evaporation gas valve, It can be utilized for gas flow control.

When the flow rate of the evaporation gas is small, the condensation can be sufficiently performed by mixing with the liquefied gas, so that the flow rate of the evaporation gas toward the mixer 50 can be increased compared with the flow rate of the evaporation gas directed to the heat exchanger 60.

On the other hand, in order to increase the condensing efficiency when the flow rate of the evaporation gas is large, the primary cooling through the heat exchange with the liquefied gas in the heat exchanger 60 and the liquefied gas injected by the spray 20a in the liquefied gas drum 20 The flow rate of the evaporative gas toward the heat exchanger 60 may be increased relative to the flow rate of the evaporative gas flowing toward the mixer 50 so as to realize secondary cooling through contact with the mixer 50. [

Of course, the flow of the evaporative gas toward the mixer 50 and the flow of the evaporative gas toward the heat exchanger 60 may be simultaneously performed, but the flow rates may be different from each other, or alternatively, only one of them may be selected.

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

Referring to FIG. 4, a liquefied gas regeneration system 1 according to a fourth embodiment of the present invention includes a liquefied gas storage tank 10, and a vaporizer train 40a. Hereinafter, the present embodiment will mainly be described with respect to different points from the above-described other embodiments, and the description omitted is replaced with the description of the other embodiments.

The vaporizer train 40a is connected to a plurality of main lines 11 connecting the liquefied gas storage tank 10 and the customer 100, respectively, and vaporizes the liquefied gas. The vaporizer train 40a may be a spatial concept including a portion that is structurally separate from other configurations, including the vaporizer 40,

The vaporizer train 40a is provided for each main line 11 and is capable of vaporizing the liquefied gas delivered from the liquefied gas storage tank 10 to the customer 100 through each main line 11. [ At this time, the main line 11 is branched into a plurality of branches downstream of the liquefied gas storage tank 10 and connected to the vaporizer trains 40a, respectively, and may be merged into one downstream of the vaporizer trains 40a. However, since the main line 11 is provided with the vaporizer trains 40a in a portion divided in parallel in the main line 11, a plurality of vaporator trains 40a may be provided in parallel.

The vaporizer train 40a is connected to a vaporization line 41 for the flow of the heat and the heat supplied to the vaporizer train 40a along the vaporization line 41 is cooled in the process of vaporizing the vaporization gas, Can be reheated and circulated by the heat exchanger (42).

Similarly to the vaporizer train 40a, the fruit line 41 may be provided in plurality, and the fruit line 41 may be connected to the vaporizer train 40a. At this time, the fruit line 41 is provided with a fruit heater 42, and the fruit heater 42 may be provided for each fruit line 41.

The fruit line 41 can communicate with each other downstream of the fruit heater 42 and upstream of the vaporizer train 40a. That is, the fruit lines 41 may be provided in parallel so as to correspond to the respective fruit heaters 42 and are integrated with each other at the downstream side of the fruit heaters 42 and then connected to the vaporizer train 40a upstream of the vaporizer train 40a. And can be connected to the vaporizer train 40a individually.

Conversely, the fruit line 41 is configured as one, but may be branched in parallel at a portion where the fruit heater 42 is provided and at a portion connected to the vaporizer train 40a. That is, the fruit line 41 is divided into a plurality of branches at the upstream side of the fruit heater 42 and connected to the fruit heater 42 respectively, and communicated with each other at the downstream of the fruit heater 42 and upstream of the vaporizer train 40a Respectively, to the vaporizer train 40a.

The plurality of the fruit heaters 42 provided in the fruit line 41 may be provided in parallel with each other and the heating line 42a may be connected to each of the fruit heaters 42. [ A plurality of heating lines 42a may be provided as many as the number of the heater heaters 42. A plurality of heating lines 42a may be provided upstream of the heaters 42 and connected to the heaters 42, Can be merged into one.

The heating line 42a may be a steam line for heating the fruit and the steam may be supplied along the heating line 42a to the side of the heating heater 42 and the steam may be supplied to the respective heating heaters 42 42 and are individually transmitted to the fruit heater 42. [ Thereafter, the steam that has exited from each of the fruit heaters 42 can be joined together and processed (reheated, etc.).

The main line 11 is connected to each of the carburetor trains 40a and the fruit line 41 is connected to each of the fruit heaters 42. In this embodiment, the vaporizer train 40a and the fruit heater 42 are provided in parallel, And the heating line 42a are connected to each other before and after the vaporizer train 40a and the heating line 41 and the heating line 42a are connected to the front and rear of the heater 42 Can be merged into one.

In this case, the flow of the liquefied gas and the flow of the liquefied gas and the steam can be evenly dispersed, and the ratio of the liquefied gas, the fruit and the steam can be optimized as the proper distribution is made.

The portion where the main line 11 is branched in parallel toward the plurality of vaporizer trains 40a and the portion where the heating line 41 and the heating line 42a branch in parallel toward the plurality of the heater heaters 42, A valve (not shown) may be provided. The valve may be provided directly at the branch point or at the upstream or downstream of the branch point, and the opening degree of the valve may be controlled according to the temperature of the liquefied gas, the temperature of the liquor, and the like.

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: main line 12: bypass line
20: liquefied gas drum 30: liquefied gas pump
40: vaporizer 41: fruit line
42: Fruit heater 43: Fruit pump
44: Fruit regulator, pressure regulator 45: Pressure regulating line
46: Fruit temperature sensor 47: Additional heater
48: high pressure gas injection unit 50: mixer
60: Heat exchanger 100: Demand source

Claims (9)

A liquefied gas storage tank for storing liquefied gas;
A main line connected to the customer from the liquefied gas storage tank;
A vaporizer provided in the main line for vaporizing the liquefied gas;
A bypass line branching from the main line;
A liquefied gas drum provided on the main line or the bypass line for temporarily storing the liquefied gas;
A mixer provided upstream of the liquefied gas drum in the main line or the bypass line and mixing the evaporated gas in the liquefied gas storage tank with the liquefied gas;
A heat exchanger provided in the main line and cooling the evaporation gas with liquefied gas; And
And an evaporative gas supply line connected to the mixer in the liquefied gas storage tank or branched to be connected to the liquefied gas drum via the heat exchanger,
Wherein the evaporation gas supply line includes:
Wherein the control unit controls the flow of the evaporative gas to the mixer when the flow rate of the evaporative gas generated in the liquefied gas storage tank is less than a predetermined value and the flow rate of the evaporative gas generated in the liquefied gas storage tank is equal to or greater than a predetermined value So that the evaporated gas flows through the heat exchanger to the liquefied gas drum. The mixer of claim 1,
Wherein at least a part of the evaporation gas is condensed using the liquefied gas and supplied to the liquefied gas drum. delete delete The method according to claim 1,
Wherein the evaporative gas supply line is branched upstream of the mixer and connected to the liquefied gas drum via the heat exchanger. 6. The method of claim 5,
And at least one evaporative gas valve provided in the evaporative gas supply line for regulating the flow rate of the evaporative gas supplied to the mixer or the liquefied gas drum. 7. The apparatus according to claim 6,
And the flow rate of the evaporation gas supplied to the mixer or the liquefied gas drum is controlled based on the flow rate of the evaporation gas generated in the liquefied gas storage tank. 7. The apparatus according to claim 6,
The evaporation gas supply line connected to the mixer is opened when the flow rate of the evaporation gas generated in the liquefied gas storage tank is less than a preset value,
Wherein the evaporating gas supply line connected to the heat exchanger and the liquefied gas drum is opened when the flow rate of the evaporation gas generated in the liquefied gas storage tank is equal to or greater than a predetermined value. A ship having the liquefied gas regeneration system of any one of claims 1, 2 and 5 to 8.

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