KR20150099362A - A Treatment System of Liquefied Gas - Google Patents

Abstract

A liquefied gas treatment system according to an embodiment of the present invention includes: an evaporation gas compressor which compresses an evaporation gas supplied from a liquefied gas storage tank; an evaporation gas liquefier which liquefies at least a part of the evaporation gas by expanding or depressurizing the evaporation gas compressed in the evaporation gas compressor; a vapor-liquid separator which separates a liquid and a vapor gas from the evaporation gas passing the evaporation gas liquefier; a first heat exchanger which exchanges heat of the evaporation gas compressed in the evaporation gas compressor with heat of the evaporation gas supplied from the liquefied gas storage tank and a vapor gas supplied from the vapor-liquid separator, and is formed as 3 streams; and a second heat exchanger which exchanges heat of the evaporation gas compressed in the evaporation gas compressor and the vapor gas supplied from the vapor-liquid separator, and is formed as 2 streams. The liquefied gas treatment system according to the present invention has the effect of maximizing liquefaction rate of the evaporation gas liquefier and has the effect of improving driving efficiency of the system, by exchanging heat of the compressed evaporation gas heat-exchanged with the evaporation gas and a fresh gas first with heat of the fresh gas secondly, or exchanging heat of the compressed evaporation gas heat-exchanged with the fresh gas first with heat of the evaporation gas and the fresh gas secondly.

Description

Description of the Related Art A Treatment System of Liquefied Gas

The present invention relates to a liquefied gas processing system.

Liquefied natural gas (Liquefied natural gas), Liquefied petroleum gas (Liquefied petroleum gas) and other liquefied gas are widely used in place of gasoline or diesel in recent technology development.

Liquefied natural gas is a liquefied natural gas obtained by refining natural gas collected from a gas field. It is a colorless and transparent liquid with almost no pollutants and high calorific value. It is an excellent fuel. On the other hand, liquefied petroleum gas is a liquid fuel made by compressing gas containing propane (C3H8) and butane (C4H10), which come from oil in oil field, at room temperature. Liquefied petroleum gas, like liquefied natural gas, is colorless and odorless and is widely used as fuel for household, business, industrial, and automotive use.

Such liquefied gas is stored in a liquefied gas storage tank installed on the ground or stored in a liquefied gas storage tank provided in a ship which is a means of transporting the ocean. The liquefied natural gas is liquefied to a volume of 1/600 The liquefaction of liquefied petroleum gas has the advantage of reducing the volume of propane to 1/260 and the content of butane to 1/230, resulting in high storage efficiency.

These liquefied gases are supplied to various customers and used. Recently, LNG carrier that uses LNG as fuel for LNG carriers that transport liquefied natural gas has been developed. The method used is applied to ships other than LNG carriers.

However, the temperature and pressure of the liquefied gas required by the customer such as the engine may be different from the state of the liquefied gas stored in the liquefied gas storage tank. Therefore, recently, research and development have been conducted on technologies for controlling the temperature and pressure of the liquefied gas stored in a liquid state to supply it to a customer.

It is an object of the present invention to provide a compressed evaporative gas-flash gas heat exchanger and a compressed evaporative gas-flash gas heat exchanger to further reduce the temperature of the compressed evaporative gas flowing into the evaporative gas liquefier, And to provide a liquefied gas processing system for improving the liquefaction rate of the gasifier and maximizing energy efficiency.

A liquefied gas processing system according to an embodiment of the present invention includes: an evaporative gas compressor for compressing an evaporative gas supplied from a liquefied gas storage tank; An evaporating gas liquefier for expanding or reducing the pressure of the evaporation gas compressed in the evaporation gas compressor to at least partially liquefy the evaporation gas; A gas-liquid separator for separating a liquid and a gas from an evaporation gas passing through the evaporation gas liquefier; A first heat exchanger formed in three streams for heat-exchanging the evaporated gas compressed in the evaporative gas compressor with the evaporated gas supplied from the liquefied gas storage tank and the gas supplied from the gas-liquid separator; And a second heat exchanger for exchanging heat between the evaporated gas compressed in the evaporative gas compressor and the gaseous gas supplied from the gas-liquid separator.

Specifically, the evaporated gas compressed in the evaporative gas compressor is subjected to first heat exchange with the evaporated gas supplied from the liquefied gas storage tank and the gas supplied from the gas-liquid separator in the first heat exchanger, and the second heat exchanger Liquid separator and the gas-liquid separator.

Specifically, the evaporated gas compressed in the evaporative gas compressor is subjected to first heat exchange with the gas gas supplied from the gas-liquid separator in the second heat exchanger, and the evaporated gas supplied from the liquefied gas storage tank in the first heat exchanger And a second heat exchange with the gas gas supplied from the gas-liquid separator.

Specifically, the gaseous gas supplied from the gas-liquid separator is subjected to first heat exchange with the compressed evaporated gas in the first heat exchanger, and second heat exchange with the compressed evaporated gas in the second heat exchanger.

Specifically, the gaseous gas heat-exchanged in the second heat exchanger may be supplied to an engine, a turbine, a boiler, a liquefier or a GCU.

Specifically, the gaseous gas heat-exchanged in the first heat exchanger may be supplied to an engine, a turbine, a boiler, a liquefier or a GCU.

The gas-liquid separator may further include a liquid recovery line connected to the liquefied gas storage tank to recover the liquid-state evaporated gas separated from the gas-liquid separator to the liquefied gas storage tank.

Specifically, the apparatus may further include a mixer for mixing the vaporized gas supplied from the liquefied gas storage tank and the gas supplied from the gas-liquid separator.

Specifically, the evaporation gas liquefier may be an expander.

Specifically, the evaporation gas liquefier may be a line Thompson valve.

The liquefied gas processing system according to the present invention is a system for performing a liquefied gas processing system in which a flash gas is subjected to a second heat exchange with a flash gas and a compressed evaporation gas subjected to a first heat exchange with a flash gas, So that the liquefaction rate of the evaporative gas liquefier is maximized and the driving efficiency of the system is improved.

1 is a conceptual diagram of a conventional liquefied gas processing system.
2 is a conceptual diagram of a liquefied gas processing system according to a first embodiment of the present invention.
3 is a cross-sectional view of a liquefied gas storage tank in a liquefied gas processing system according to a first embodiment of the present invention.
4 is a graph showing the power consumption for the flow rate of the evaporative gas compressor in a general liquefied gas processing system.
5 is a conceptual diagram of a liquefied gas processing system according to a second embodiment of the present invention.
6 is a cross-sectional view of a liquefied gas storage tank in a liquefied gas processing system according to a second embodiment of the present invention.
7 is a conceptual diagram of a liquefied gas processing system according to a third embodiment of the present invention.
8 is a graph showing the power consumption for the flow rate of the evaporative gas compressor in a general liquefied gas processing system.
9 is a conceptual diagram of a liquefied gas processing system according to a fourth embodiment of the present invention.
10 is a conceptual diagram of a liquefied gas processing system according to a fifth embodiment of the present invention.
11 is a conceptual diagram of a liquefied gas processing system according to a sixth embodiment of the present invention.
12 is a conceptual diagram of a liquefied gas processing system according to a seventh embodiment of the present invention.
13 is a conceptual diagram of a liquefied gas processing system according to an eighth embodiment of the present invention.
14 is a conceptual diagram of a liquefied gas processing system according to a ninth embodiment of the present invention.
15 is a conceptual diagram of a liquefied gas processing system according to a tenth embodiment of the present invention.
16 is a conceptual diagram of a liquefied gas processing system according to an eleventh embodiment of the present invention.
17 is a conceptual diagram of a liquefied gas processing system according to a twelfth embodiment of the present invention.
18 is a conceptual diagram of a liquefied gas processing system according to a thirteenth embodiment of the present invention.

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

1 is a conceptual diagram of a conventional liquefied gas processing system.

1, a conventional liquefied gas processing system 1 includes a liquefied gas storage tank 10, a liquefied gas consumer 20, a pump 30, and a liquefied gas heat exchanger 40. In this case, the liquefied gas consumer 20 may be a gaseous fuel engine, which is a consumer of high-pressure liquefied gas, or a dual fuel engine, which is a consumer of low-pressure liquefied gas. The pump 30 may include a booster pump 31 and a high- 32). Here, the liquefied gas may be connected to the liquefied gas supply line from the liquefied gas storage tank 10 to the pump 30, the liquefied gas heat exchanger 40, and the liquefied gas consumer 20.

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

The conventional liquefied gas processing system 1 is a system in which a liquefied gas in a liquid state is taken out of a liquefied gas storage tank 10 and is pressurized through a boosting pump 31 and a high pressure pump 32 and then supplied to a liquefied gas heat exchanger 40 And is supplied to the liquefied gas consumer 20 by heating with glycol water or the like.

However, in this case, since only the liquefied gas in the liquid state stored in the liquefied gas storage tank 10 is used, the evaporated gas naturally generated in the liquefied gas storage tank 10 by the external heat penetration is stored in the liquefied gas storage tank 10 And discharged to the outside along the evaporation gas discharge line 16 (made up of the evaporation gas supply line in the embodiment of the present invention) to lower the internal pressure. Therefore, the conventional liquefied gas processing system 1 can not utilize the evaporation gas at all, resulting in a waste of energy.

FIG. 3 is a cross-sectional view of a liquefied gas storage tank in a liquefied gas processing system according to the first embodiment of the present invention, and FIG. 4 is a cross- FIG. 5 is a graph showing the power consumption for the flow rate of the evaporative gas compressor in the gas treatment system. FIG.

2, the liquefied gas processing system 2 according to the first embodiment of the present invention includes a liquefied gas storage tank 10, an evaporative gas compressor 50, an evaporative gas heat exchanger 60, (70), an evaporation gas liquefier (80), and a gas-liquid separator (90). In the embodiment of the present invention, the liquefied gas storage tank 10, the liquefied gas consumer 20, and the like are denoted by the same reference numerals as those in the conventional liquefied gas processing system 1, It does not.

X, X ', Y, and Y' shown in FIG. 2 will be described in the fifth to twelfth embodiments described with reference to FIG. 10 to FIG.

The liquefied gas storage tank 10 stores liquefied gas to be supplied to the liquefied gas consumer 20. The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, wherein the liquefied gas storage tank 10 may have the form of a pressure tank.

3, the liquefied gas storage tank 10 includes an outer tank 11, an inner tank 12, and a heat insulating portion 13. As shown in Fig. The outer tank 11 is formed of an outer wall of the liquefied gas storage tank 10, and may be formed of steel, and may have a polygonal cross section.

The tanks 12 are provided inside the tanks 11 and can be supported and supported inside the tanks 11 by means of a support 14. At this time, the support 14 may be provided at the lower end of the inner tank 12, and may be provided at the side of the inner tank 12 in order to suppress the lateral movement of the inner tank 12. [

The bath tank 12 may be made of stainless steel and designed to withstand a pressure of 5 bar to 10 bar (for example 6 bar). The reason why the inner tank 12 is designed to withstand such a constant pressure is that the inner pressure of the inner tank 12 is raised as the liquefied gas provided in the inner tank 12 is evaporated and the evaporated gas is generated It is because.

A baffle 15 may be provided in the inner tank 12. [ The baffle 15 means a plate in the form of a lattice and the baffle 15 is installed so that the pressure inside the tank 12 can be evenly distributed to prevent the tank 12 from being subjected to concentrated pressure .

The heat insulating portion 13 is provided between the inner tank 12 and the outer tank 11 and can prevent the external heat energy from being transmitted to the inner tank 12. [ At this time, the heat insulating portion 13 may be in a vacuum state. By forming the adiabatic portion 13 in a vacuum, the liquefied gas storage tank 10 can more efficiently withstand higher pressures as compared to conventional tanks. For example, the liquefied gas storage tank 10 can sustain a pressure of 5 to 20 bar through the vacuum insulation 13.

As described above, the present embodiment uses a pressure tank type liquefied gas storage tank 10 having a vacuum type heat insulating portion 13 between the outer tank 11 and the inner tank 12, thereby minimizing the generation of evaporated gas It is possible to prevent the problems such as breakage of the liquefied gas storage tank 10 even if the internal pressure is increased.

In the present embodiment, the evaporation gas generated in the liquefied gas storage tank 10 is supplied to the evaporation gas compressor 50 to be used for heating the evaporation gas, or the evaporation gas is vaporized and pressurized, The vaporized gas can be efficiently used.

Here, a forcing vaporizer 26 may be provided downstream of the liquefied gas storage tank 10, and the forced vaporizer 26 may be operated when the flow rate of the evaporation gas is insufficient and supplied to the liquefied gas consumer 20 It is possible to increase the flow rate of the evaporating gas. That is, the forced vaporizer 26 is provided upstream of the mixer 70 on the evaporation gas supply line 16 to vaporize the liquefied gas in the liquefied gas storage tank 10 and supply it to the evaporative gas compressor 50 in the gaseous liquefied gas Can be supplied.

The liquefied gas consumer 20 is driven through evaporative gas supplied from the liquefied gas storage tank 10 and flash gas to generate power. At this time, the liquefied gas consumer 20 is a high-pressure engine, and may be a gas fuel engine (for example, MEGI).

As a piston (not shown) in the cylinder (not shown) reciprocates by the combustion of the liquefied gas, the liquefied gas consumer 20 rotates a crankshaft (not shown) connected to the piston, The shaft (not shown) to be connected can be rotated. Therefore, as the propeller (not shown) connected to the shaft rotates when the liquefied gas consumer 20 is driven, the hull can move forward or backward.

Of course, in this embodiment, the liquefied gas consumer 20 may be an engine for driving the propeller, but it may be an engine for generating power or an engine for generating other power. That is, the present embodiment does not particularly limit the kind of the liquefied gas consumer 20. However, the liquefied gas consumer 20 may be an internal combustion engine that generates a driving force by the combustion of the evaporative gas and the flash gas.

The liquefied gas consumer 20 is supplied with the evaporated gas and the flash gas pressurized by the evaporative gas compressor 50 to obtain the driving force. The state of the evaporated gas and flash gas supplied to the liquefied gas consumer 20 may vary depending on the state required by the liquefied gas consumer 20.

Or the liquefied gas consumer 20 may be a dual fuel engine in which evaporation gas and oil are selectively supplied without being mixed with the evaporation gas and oil. The dual fuel engine is selectively supplied with the evaporation gas or oil in order to prevent the mixing of the two materials having different combustion temperatures to prevent the efficiency of the liquefied gas consumer 20 from deteriorating.

An evaporative gas supply line 16 for transferring evaporative gas may be provided between the liquefied gas storage tank 10 and the liquefied gas consumer 20 and the evaporative gas supply line 16 may be provided with a forced vaporizer 26, The evaporation gas heat exchanger 60 and the evaporation gas compressor 50 are installed to supply the evaporation gas to the liquefied gas consumer 20. The evaporation gas supply line 16 is connected to the evaporation gas compressor 50, The evaporated gas return line 16A may be branched between the liquefied gas consumer 20 and the liquefied gas consumer 20. The evaporation gas return line 16A may be provided with an evaporation gas heat exchanger 60, an evaporation gas liquefier 80, and the like, and may be supplied to the gas-liquid separator 90.

At this time, a fuel supply valve (not shown) is provided in the evaporation gas supply line 16 and the evaporation gas return line 16A so that the supply amount of the evaporation gas can be adjusted according to the opening degree of the fuel supply valve.

The evaporative gas compressor (50) pressurizes the evaporative gas generated in the liquefied gas storage tank (10). The evaporation gas compressor 50 can pressurize the evaporation gas generated and discharged from the liquefied gas storage tank 10 and supply it to the evaporation gas heat exchanger 60 or the liquefied gas consumer 20.

The plurality of evaporation gas compressors (50) can pressurize the evaporation gas at multiple stages. For example, five evaporation gas compressors 50 may be provided so that the evaporation gas is pressurized in five stages. The five-stage pressurized evaporated gas can be pressurized to 200 to 400 bar and supplied to the liquefied gas consumer 20 through the high-pressure evaporative gas supply line 24.

Here, the evaporation gas return line 16A may be branched between the evaporation gas compressor 50 and the liquefied gas consumer 20 on the evaporation gas supply line 16, and may be connected to the evaporation gas heat exchanger 60. At this time, a valve (not shown) may be provided on the evaporation gas supply line 16 at the branch point to the evaporation gas heat exchanger 60, and the valve may be a flow rate of the evaporation gas supplied to the liquefied gas consumer 20 The flow rate of the evaporative gas supplied to the evaporative gas heat exchanger (60) through the evaporative gas compressor (50) can be controlled, and can be a three - way valve.

Between the plurality of evaporative gas compressors 50, an evaporative gas cooler (not shown) may be provided. When the evaporation gas is pressurized by the evaporation gas compressor 50, since the temperature may also rise with the pressure increase, this embodiment can lower the temperature of the evaporation gas again by using the evaporation gas cooler. The evaporative gas cooler may be installed in the same number as the evaporative gas compressor 50, and each evaporative gas cooler may be provided downstream of each evaporative gas compressor 50.

As the evaporation gas compressor 50 pressurizes the evaporation gas, the evaporation gas can be in a state where the pressure rises and the boiling point rises and can be liquefied even at a relatively high temperature. Therefore, this embodiment can increase the pressure of the evaporation gas to the evaporation gas compressor 50, so that the evaporation gas can be easily liquefied.

The liquefied gas processing system 2 according to the first embodiment of the present invention may further include a compressor front-end heat exchanger 51.

The compressor front end heat exchanger 51 may be provided on the evaporation gas supply line 16 and may supply a constant evaporation gas to the evaporation gas compressor 50 at an arbitrary temperature. Specifically, the compressor front end heat exchanger 51 is provided on the evaporation gas supply line 16 and may be provided between the evaporation gas compressor 50 and the evaporation gas heat exchanger 60.

The liquefied gas processing system 2 according to the first embodiment of the present invention is a system in which the compressed evaporation gas supplied through the evaporation gas return line 16A, the evaporation gas supplied from the evaporation gas storage tank 10, The temperature of the evaporative gas flowing into the evaporative gas compressor 50 or the flow rate of the evaporative gas may fluctuate irregularly according to the operating conditions such as the flash gas supplied from the evaporator 90.

The temperature or the flow rate of the evaporative gas discharged from the evaporative gas compressor 50 to the consumer 20 may also be varied if the temperature or the flow rate of the evaporative gas flowing into the evaporative gas compressor 50 fluctuates.

When the consumer 20 receives the evaporation gas with a large fluctuation in the temperature or the flow rate without being constantly supplied with the temperature or the flow rate requested by the consumer 20 from the evaporation gas compressor 50, It can fall and cause serious problems in driving.

Therefore, in the embodiment of the present invention, in order to keep the temperature of the evaporation gas flowing into the evaporation gas compressor 50 or the flow rate of the evaporation gas constant, a compressor front-end heat exchanger 51 is provided at the front end of the evaporation- And the evaporation gas compressor (50) can supply a constant temperature or a constant flow rate to the evaporative gas compressor (50).

Therefore, in the embodiment of the present invention, the stable supply of the evaporation gas with the temperature and the flow rate of the evaporation gas can be made possible by the customer 20, thereby increasing the reliability of the liquefied gas processing system 2, And the durability of the customer 20 can be improved.

The compressor front-end heat exchanger (51) is provided on the evaporation gas supply line (16) and can exchange heat with the external heat source and the evaporation gas supplied to the evaporation gas compressor (50). The external heat source may be a heat exchange medium used in an evaporative gas cooler (not shown) provided at the rear end of the evaporative gas compressor 50, and may be a liquefied gas heat exchanger 40 provided on the liquefied gas supply line 21, , And may be a heat source other than the liquefied gas processing system 2. [ However, the external heat source is not limited to those described above, and may be variously selected.

The compressor front-end heat exchanger (51) is provided at the upstream end of the evaporative gas compressor (50) to preheat the evaporative gas supplied to the evaporative gas compressor (50).

Since the evaporated gas discharged from the liquefied gas storage tank 10 corresponds to about -120 DEG C, it corresponds to an ultra-low temperature. When the extremely low temperature evaporated gas is directly introduced into the evaporative gas compressor 50, there is a possibility that the evaporative gas compressor 50 is broken, and the operation efficiency may be lowered.

Therefore, in the liquefied gas processing system 2 according to the first embodiment of the present invention, the compressor front-end heat exchanger 51 can serve as a preheater, thereby preventing breakage of the evaporative gas compressor 50, The operating efficiency of the gas compressor (50) can be increased.

Further, the liquefied gas processing system 2 according to the first embodiment of the present invention allows the evaporation gas compressor 50 to be used as a conventional evaporation gas compressor 50 instead of the cryogenic compressor, The width of the selection of the gas compressor 50 can be widened, so that it is possible to manufacture the gas compressor 50 with a flexible design.

The compressor front-end heat exchanger 51 is provided with an oil / radio transceiver and is provided with a vapor-phase gas temperature value or a vapor gas flow rate value measured from a temperature sensor (not shown) or a flow rate sensor And can transmit any evaporation gas flow rate value that can be set according to the design to the flow rate control sensor.

The liquefied gas processing system 2 according to the first embodiment of the present invention may further include a temperature sensing sensor (not shown) and a flow rate control sensor (not shown).

The temperature sensor is provided between the compressor front-end heat exchanger 51 and the evaporation gas heat exchanger 60 to measure the temperature of the evaporation gas flowing into the compressor front-end heat exchanger 51.

The temperature sensor may be disposed between the compressor front-end heat exchanger 51 and the evaporative gas compressor 50 to measure the temperature of the evaporative gas supplied to the evaporative gas compressor 50.

The temperature sensing sensor includes an oil and radio transmitter and is provided with an evaporation gas temperature measurement value supplied to the evaporation gas compressor 50 or an evaporation gas temperature measurement value introduced into the compressor front end heat exchanger 51, Can be transmitted to the sub-heat exchanger (51) through a radio or wireless method.

The flow rate control sensor is provided between the compressor front-end heat exchanger 51 and the evaporation gas heat exchanger 60 to measure the flow rate of the evaporative gas flowing into the compressor front-end heat exchanger 51, To control the flow rate of the evaporative gas flowing into the compressor front-end heat exchanger (51).

The flow rate control sensor is provided between the compressor front-end heat exchanger 51 and the evaporative gas compressor 50 to measure the flow rate of the evaporative gas introduced into the evaporative gas compressor 50, It is possible to control the flow rate of the evaporative gas flowing into the evaporator 50.

The flow rate control sensor is provided with an oil and radio transmission device so that the flow rate value of the evaporation gas supplied to the evaporation gas compressor 50 or the flow rate value of the evaporation gas flowing into the compressor front end heat exchanger 51, Can be transmitted to the sub-heat exchanger (51) through a radio or wireless method.

Also, the flow rate sensor may include an oil and radio receiver and may receive an arbitrary flow rate value from the compressor front-end heat exchanger 51 to control the on-off valve. Here, the flow rate sensor can control the flow rate of the evaporation gas supplied to the evaporation gas compressor (50) or the flow rate of the evaporation gas supplied to the compressor front end heat exchanger (51) through the control of the opening / closing valve.

The evaporation gas heat exchanger 60 is provided between the liquefied gas storage tank 10 and the evaporation gas compressor 50 on the evaporation gas supply line 16 and is provided between the evaporation gas pressurized in the evaporation gas compressor 50 and the liquefied gas storage The evaporation gas supplied from the tank 10 can be heat-exchanged. The evaporated gas heat-exchanged in the evaporative gas heat exchanger (60) may be supplied to the evaporative gas liquefier (80) or the evaporative gas compressor (50). That is, the evaporated gas recovered to the evaporative gas liquefier 80 and the evaporated gas newly supplied from the liquefied gas storage tank 10 after being multi-stage pressurized by the evaporative gas compressor 50 are heat-exchanged in the evaporative gas heat exchanger 60 do.

The mixer 70 is provided upstream of the evaporation gas heat exchanger 60 on the evaporation gas supply line 16 and is supplied with the flash gas that is supplied from the liquefied gas storage tank 10 and is recovered in the gas- Can be introduced. The mixer (70) may be in the form of a pressure tank, which is space for storing the evaporating gas and the flash gas. Here, the evaporated gas and the flash gas mixed in the mixer 70 are supplied to the evaporative gas heat exchanger 50.

The evaporation gas liquefier 80 is pressurized in the evaporative gas compressor 50 to liquefy at least a portion of the evaporated gas heat exchanged in the evaporative gas heat exchanger 60 with a reduced pressure or an expansion key. For example, the evaporation gas liquefier 80 can reduce the pressure of the evaporation gas to 1 bar to 10 bar, and the evaporation gas can be liquefied and reduced to 1 bar when transferred to the liquefied gas storage tank 10, The cooling effect can be achieved.

Here, the evaporated gas pressurized in the evaporative gas compressor (50) is heat-exchanged with the evaporated gas supplied from the liquefied gas storage tank (10) in the evaporative gas heat exchanger (60) The discharge pressure can be maintained. In this embodiment, the evaporation gas is condensed by using the evaporation gas liquefier 80 so that the evaporation gas is allowed to cool, and the evaporation gas can be liquefied. At this time, the greater the pressure range to be depressurized, the greater the cooling effect of the evaporative gas. For example, the evaporative gas liquefier 80 can reduce the evaporated gas pressurized to 300 bar by the evaporative gas compressor 50 to 1 bar.

Evaporative gas liquefier 80 may be a line Thompson valve. Alternatively, the evaporative gas liquefier 80 may comprise an inflator (not shown). In the case of the Row Thompson valve, depressurization can effectively cool the evaporated gas so that at least some of the evaporated gas is liquefied. Here, the inflator may also be made of an expander (not shown).

On the other hand, the inflator can be driven without using any extra power, and in particular, the efficiency of the liquefied gas processing system 2 can be improved by utilizing the generated power as electric power for driving the evaporative gas compressor 50. The power transmission may be accomplished by, for example, a gear connection or an electric conversion and the like.

A gas-liquid separator 90 separates the gas from the evaporated gas that has been depressurized or expanded in the evaporative gas liquefier 80. In the gas-liquid separator 90, the evaporated gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas can be recovered as flash gas upstream of the evaporative gas compressor 50.

Here, the evaporation gas supplied to the gas-liquid separator 90 may be decompressed and cooled in the evaporation gas liquefier 80. For example, in the evaporative gas compressor (50), the evaporation gas may be multi-stage pressurized to have a pressure of 200 bar to 400 bar, and the temperature may be around 45 degrees. The evaporated gas raised to a temperature of about 45 degrees is recovered by the evaporation gas heat exchanger 60 and is heat-exchanged with the evaporation gas of about -100 degrees supplied from the liquefied gas storage tank 10, And is supplied to the evaporation gas liquefier 80. At this time, in the evaporating gas liquefier 80, the evaporated gas is cooled by the reduced pressure and can have a pressure of about 1 bar and a temperature of about -162.3 degrees.

As described above, in this embodiment, since the evaporation gas supplied to the gas-liquid separator 90 is reduced in pressure by the evaporation gas liquefier 80 to have a temperature lower than -162 degrees, about 30 to 40% of the evaporation gas can be liquefied have.

In this embodiment, the liquefied evaporated gas is recovered to the liquefied gas storage tank 10, and the flash gas generated in the gas-liquid separator 90 is recovered to the mixer 70 without discarding the evaporated gas and the flash gas, Gas compressor 50, and then supplied to the liquefied gas consumer 20.

Liquid separator 90 separates the vaporized gas into a liquid and a gas, the liquefied vaporized gas and the flash gas are respectively passed through the liquid recovery line 19 and the gas recovery line 17 to the liquefied gas storage tank 10, (70). ≪ / RTI >

The liquid recovery line 19 is connected from the gas-liquid separator 90 to the liquefied gas storage tank 10 to recover the vaporized liquid state to the liquefied gas storage tank 10 and the gas recovery line 17 is connected to the gas- 90 to the mixer 70 upstream of the evaporative gas compressor 50 to recover the flash gas upstream of the evaporative gas compressor 50 to prevent the flash gas from being wasted and wasted.

At this time, the flash gas may be cooled to a temperature of -162.3 DEG C by being decompressed by the evaporation gas liquefier 80 as mentioned above. The flash gas and the -100 degree evaporation gas generated in the liquefied gas storage tank are mixed in the mixer 70 And flows into the evaporation gas heat exchanger 60 as evaporation gas of -110 to -120 degrees (about-114 degrees).

Accordingly, the 45-degree evaporated gas recovered along the evaporated-gas return line 16A, which is branched between the evaporated-gas compressor 50 and the liquefied-gas consumer 20 and connected to the evaporated-gas heat exchanger 60, Lt; RTI ID = 0.0 > -110 < / RTI > to < RTI ID = 0.0 > -120 < / RTI > This allows additional cooling of the evaporated gas to be achieved when the flash gas is not recovered (45 degrees of evaporation gas versus -100 degrees of evaporation and heat exchange).

Therefore, the evaporated gas discharged from the evaporative gas heat exchanger 60 and flowing into the evaporative gas liquefier 80 may be about -112 degrees lower than the case where there is no circulation of the flash gas (about -97 degrees) When the pressure is reduced by the liquefier 80, it can be cooled to about -163.7 degrees. In this case, more evaporative gas can be liquefied by the evaporative gas liquefier 80 and recovered to the liquefied gas storage tank 10 than when the flash gas is not circulated.

Therefore, in this embodiment, the gaseous evaporative gas in the evaporated gas cooled through the evaporative gas liquefier 80 is separated into flash gas in the gas-liquid separator 90 and supplied to the evaporative gas heat exchanger 60, The liquefaction efficiency of the evaporation gas can be increased to 60% or more by sufficiently lowering the temperature of the evaporation gas recovered from the compressor 50 to the evaporation gas heat exchanger 60 and the evaporation gas liquefier 80. [

In this embodiment, not only the evaporated gas from the liquefied gas storage tank 10 but also the flash gas is mixed with the evaporated gas and flows into the evaporated gas compressor 50, so that a constant flow rate or more is supplied to the evaporated gas compressor 50 So that the driving efficiency can be improved.

As shown in the graph of FIG. 4, in a general evaporative gas compressor, when the flow rate increases in the section B, the power consumption increases proportionally. This means that a large amount of power is required to compress the evaporated gas at a large flow rate. In this case, the section B may be a section having a larger flow rate than the predetermined value (reference value determining the section A and the section B) which is determined according to the specifications of the evaporative gas compressor and the driving conditions.

On the other hand, when the flow rate of the evaporating gas flowing into the evaporative gas compressor is smaller than the preset value, the consumption power is not decreased even if the flow rate is reduced in the A period. This is because there is a risk of surging when a certain volume of evaporation gas is not introduced into the evaporation gas compressor, and when the evaporation gas flow rate flowing into the evaporation gas compressor 50 is less than the predetermined value, The volume of the evaporated gas introduced into the evaporative gas compressor 50 must be maintained at a predetermined value or more by recycling to generate power for recycling.

However, since the evaporative gas compressor 50 of this embodiment can introduce the flash gas into the evaporative gas compressor 50 together with the evaporative gas, even if the flow rate of the evaporative gas decreases in the section A where the evaporative gas flow rate is lower than the predetermined value Since the volume required by the evaporative gas compressor (50) can be satisfied through the flash gas, power consumption can be reduced as the evaporative gas flow rate is reduced. That is, in the evaporative gas compressor 50 of the present embodiment, the power consumption can be proportionally reduced when the flow rate is reduced in the section A.

Therefore, in this embodiment, when the amount of the evaporation gas is small, the amount of the flash gas is controlled to reduce the recycle control of the evaporation gas compressor 50, and the power required for the low-load operation of the evaporation gas compressor 50 Can be saved.

In the evaporative gas compressor (50) of this embodiment, the power consumption increases as the flow rate increases in the section B. This is because a large amount of power is required to compress a larger amount of evaporation gas. However, since the present embodiment includes a configuration for circulating the flash gas, irrespective of the increase in the power consumption of the evaporative gas compressor 50 depending on the flow rate of the evaporative gas, the efficiency of re-liquefaction of the evaporative gas is greatly improved .

As described above, in the present embodiment, the evaporation gas generated in the liquefied gas storage tank 10 is pressurized and supplied to the liquefied gas consumer 20 by the infiltration of external heat, or the flash gas is circulated to the evaporative gas compressor 50, Gas to be supplied to the liquefied gas consumer 20 so as to prevent the evaporation gas from being discarded, so that the fuel can be saved. Further, the liquefaction efficiency can be maximized by further cooling the evaporation gas with the flash gas, A predetermined flow rate or more is supplied to the evaporative gas compressor 50 to minimize the recycle control, thereby improving the driving efficiency.

FIG. 5 is a conceptual diagram of a liquefied gas processing system according to a second embodiment of the present invention, and FIG. 6 is a sectional view of a liquefied gas storage tank in a liquefied gas processing system according to a second embodiment of the present invention.

5, the liquefied gas processing system 3 according to the second embodiment of the present invention includes a liquefied gas storage tank 10, an evaporative gas compressor 50, an evaporative gas heat exchanger 60, A liquefier 80 and a gas-liquid separator 90. The liquefied gas storage tank 10, the liquefied gas consumer 20 and the like in the second embodiment of the present invention are the same as those in the conventional liquefied gas processing system 1 The same reference numerals are used for the respective constructions and convenience, but they are not necessarily construed to refer to the same constructions.

The X, X ', Y, Y', Z, and Z 'shown in FIG. 5 will be described in the fifth to twelfth embodiments described with reference to FIGS. 10 to 17. FIG.

The liquefied gas storage tank 10 stores liquefied gas to be supplied to the liquefied gas consumer 20. The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, wherein the liquefied gas storage tank 10 may have the form of a pressure tank.

6, the liquefied gas storage tank 10 includes an outer tank 11, an inner tank 12, and a heat insulating portion 13. As shown in Fig. The outer tank 11 is formed of an outer wall of the liquefied gas storage tank 10, and may be formed of steel, and may have a polygonal cross section.

The tanks 12 are provided inside the tanks 11 and can be supported and supported inside the tanks 11 by means of a support 14. At this time, the support 14 may be provided at the lower end of the inner tank 12, and may be provided at the side of the inner tank 12 in order to suppress the lateral movement of the inner tank 12. [

The bath tank 12 may be made of stainless steel and designed to withstand a pressure of 5 bar to 10 bar (for example 6 bar). The reason why the inner tank 12 is designed to withstand such a constant pressure is that the inner pressure of the inner tank 12 is raised as the liquefied gas provided in the inner tank 12 is evaporated and the evaporated gas is generated It is because.

A baffle (not shown) may be provided in the inner tank 12. The baffle means a plate in the form of a lattice. As the baffle is installed, the pressure inside the tank 12 can be evenly distributed to prevent the tank 12 from being subjected to concentrated pressure.

The heat insulating portion 13 is provided between the inner tank 12 and the outer tank 11 and can prevent the external heat energy from being transmitted to the inner tank 12. [ At this time, the heat insulating portion 13 may be in a vacuum state. By forming the adiabatic portion 13 in a vacuum, the liquefied gas storage tank 10 can more efficiently withstand higher pressures as compared to conventional tanks. For example, the liquefied gas storage tank 10 can sustain a pressure of 5 to 20 bar through the vacuum insulation 13.

As described above, the present embodiment uses a pressure tank type liquefied gas storage tank 10 having a vacuum type heat insulating portion 13 between the outer tank 11 and the inner tank 12, thereby minimizing the generation of evaporated gas It is possible to prevent the problems such as breakage of the liquefied gas storage tank 10 even if the internal pressure is increased.

In the present embodiment, the evaporation gas generated in the liquefied gas storage tank 10 is supplied to the evaporation gas compressor 50 to be used for heating the evaporation gas, or the evaporation gas is vaporized and pressurized, The vaporized gas can be efficiently used.

Here, a forcing vaporizer (not shown) may be provided downstream of the liquefied gas storage tank 10, and the forced vaporizer is operated when the flow rate of the evaporation gas is insufficient, and is supplied to the liquefied gas consumer 20 The flow rate of the evaporation gas can be increased. That is, the forced vaporizer is provided on the evaporation gas supply line 16 upstream of the evaporation gas heat exchanger 60 to vaporize the liquefied gas in the liquefied gas storage tank 10 and supply it to the evaporation gas compressor 50 in the gaseous liquefied gas Can be supplied.

The liquefied gas consumer 20 is driven through the evaporation gas supplied from the liquefied gas storage tank 10 to generate power. At this time, the liquefied gas consumer 20 is a high-pressure engine, and may be a gas fuel engine (for example, MEGI).

As a piston (not shown) in the cylinder (not shown) reciprocates by the combustion of the liquefied gas, the liquefied gas consumer 20 rotates a crankshaft (not shown) connected to the piston, The shaft (not shown) to be connected can be rotated. Therefore, as the propeller (not shown) connected to the shaft rotates when the liquefied gas consumer 20 is driven, the hull can move forward or backward.

Of course, in this embodiment, the liquefied gas consumer 20 may be an engine for driving the propeller, but it may be an engine for generating power or an engine for generating other power. That is, the present embodiment does not particularly limit the kind of the liquefied gas consumer 20. However, the liquefied gas consumer 20 may be an internal combustion engine that generates a driving force by the combustion of the evaporative gas and the flash gas.

The liquefied gas consumer 20 is supplied with the evaporated gas pressurized by the evaporative gas compressor 50 to obtain the driving force. The state of the evaporated gas supplied to the liquefied gas consumer 20 may vary depending on the state required by the liquefied gas consumer 20.

Between the liquefied gas storage tank 10 and the liquefied gas consumer 20, an evaporation gas supply line 16 for transferring the evaporation gas may be installed. The evaporation gas supply line 16 is provided with a forced vaporizer, an evaporation gas heat exchanger 60 and an evaporation gas compressor 50 so that the evaporation gas can be supplied to the liquefied gas consumer 20 and the evaporation gas supply line 16 The evaporative gas return line 16A that branches off between the evaporative gas compressor 50 and the liquefied gas consumer 20 may be installed. The evaporation gas return line 16A is provided with an evaporation gas liquefier 80 and a gas-liquid separator 90 so that the evaporation gas can be supplied to the gas-liquid separator 90.

At this time, a fuel supply valve (not shown) is provided in the evaporation gas supply line 16 and the evaporation gas return line 16A so that the supply amount of the evaporation gas can be adjusted according to the opening degree of the fuel supply valve.

The evaporative gas compressor (50) pressurizes the evaporative gas generated in the liquefied gas storage tank (10). The evaporation gas compressor 50 can pressurize the evaporation gas generated and discharged from the liquefied gas storage tank 10 and supply it to the evaporation gas heat exchanger 60 or the liquefied gas consumer 20.

The plurality of evaporation gas compressors (50) can pressurize the evaporation gas at multiple stages. For example, five evaporation gas compressors 50 may be provided so that the evaporation gas is pressurized in five stages. The five-stage pressurized evaporated gas can be pressurized to 200 to 400 bar and supplied to the liquefied gas consumer 20 through the high-pressure evaporative gas supply line 24.

Here, the evaporation gas return line 16A may be branched between the evaporation gas compressor 50 and the liquefied gas consumer 20, and may be connected to the evaporation gas heat exchanger 60. At this time, a valve (not shown) may be provided on the evaporation gas supply line 16 at the branch point to the evaporation gas heat exchanger 60, and the valve may be a flow rate of the evaporation gas supplied to the liquefied gas consumer 20 The flow rate of the evaporative gas supplied to the evaporative gas heat exchanger (60) through the evaporative gas compressor (50) can be controlled, and can be a three - way valve.

Between the plurality of evaporative gas compressors 50, an evaporative gas cooler (not shown) may be provided. When the evaporation gas is pressurized by the evaporation gas compressor 50, since the temperature may also rise with the pressure increase, this embodiment can lower the temperature of the evaporation gas again by using the evaporation gas cooler. The evaporative gas cooler may be installed in the same number as the evaporative gas compressor 50, and each evaporative gas cooler may be provided downstream of each evaporative gas compressor 50.

As the evaporation gas compressor 50 pressurizes the evaporation gas, the evaporation gas can be in a state where the pressure rises and the boiling point rises and can be liquefied even at a relatively high temperature. Therefore, this embodiment can increase the pressure of the evaporation gas to the evaporation gas compressor 50, so that the evaporation gas can be easily liquefied.

The liquefied gas processing system 3 according to the second embodiment of the present invention may further include a compressor front end heat exchanger 51, a temperature measurement sensor (not shown) or a flow rate control sensor (not shown) . However, details thereof are similar to those of the liquefied gas processing system 2 according to the first embodiment, and therefore, the description will be omitted.

The evaporation gas heat exchanger (60) is provided between the liquefied gas storage tank (10) and the evaporative gas compressor (50) on the evaporation gas supply line (16). The evaporation gas heat exchanger 60 is capable of exchanging heat between the evaporation gas pressurized in the evaporation gas compressor 50 and the evaporation gas supplied from the liquefied gas storage tank 10 and the flash gas separated from the gas-liquid separator 90.

That is, the evaporation gas heat exchanger 60 is connected to the vaporized gas recovered along the evaporated gas return line 16A which is pressurized in the evaporated gas compressor 50 and branched at the upstream of the liquefied gas consumer and the evaporated gas recovered from the liquefied gas storage tank 10 Exchanges the supplied evaporation gas. The evaporation gas heat exchanger 60 exchanges heat between the evaporated gas that has been pressurized in the evaporative gas compressor 50 and recovered along the evaporative gas return line 16A and the flash gas supplied through the gas recovery line 17.

At this time, the evaporation gas heat exchanger 60 can cool the evaporation gas recovered along the evaporation gas return line 16A to the evaporation gas supplied from the liquefied gas storage tank 10, Lt; RTI ID = 0.0 > flash gas. ≪ / RTI > In this case, the evaporated gas recovered along the evaporated gas return line 16A is primarily cooled by the evaporated gas discharged from the liquefied gas storage tank 10, and can be cooled secondarily by the flash gas.

The evaporation gas heat exchanger (60) supplies the evaporation gas supplied from the liquefied gas storage tank (10) to the evaporation gas compressor (50), and the evaporation gas secondarily cooled by the evaporation gas and the flash gas is supplied to the evaporation gas liquefier (80). In this case, since the evaporation gas supplied to the evaporation gas liquefier 80 is cooled not only by the evaporation gas but also by the flash gas, the liquefaction efficiency due to the reduced pressure can be greatly increased.

The flash gas passing through the evaporative gas heat exchanger (60) can be discharged to the outside. Here, the flash gas may be supplied to a gas combustion unit (not shown) for burning the fuel and burned. At this time, a flash gas discharge line 18 is formed in the evaporation gas heat exchanger 60, and the flash gas discharge line 18 can be connected to the gas combustion unit.

Accordingly, the evaporation gas supplied to the evaporation gas compressor 50 in the evaporation gas heat exchanger 60 is heated, the evaporation gas supplied to the gas-liquid separator 90 is cooled, and is supplied from the gas-liquid separator 90 and discharged The flash gas can be heated.

The evaporation gas liquefier 80 is pressurized in the evaporation gas compressor 50 to decompress or expand the evaporated gas heat exchanged in the evaporation gas heat exchanger 60 to liquefy at least a part thereof. For example, the evaporation gas liquefier 80 can reduce the evaporation gas to about 3 bar, and the evaporation gas can be cooled when the pressure is reduced.

Here, the evaporated gas pressurized in the evaporative gas compressor (50) is heat-exchanged with the evaporated gas supplied from the liquefied gas storage tank (10) in the evaporative gas heat exchanger (60) The discharge pressure can be maintained. This embodiment uses the evaporation gas liquefier 80 to decompress or expand the evaporation gas so that the evaporation gas is allowed to cool, thereby liquefying the evaporation gas. At this time, the greater the pressure range to be depressurized, the greater the cooling effect of the evaporative gas. For example, the evaporative gas liquefier 80 may reduce the evaporated gas pressurized to 300 bar by the evaporative gas compressor 50 to 3 bar.

Evaporative gas liquefier 80 may be a line Thompson valve. In the case of the Row Thompson valve, depressurization can effectively cool the evaporated gas so that at least some of the evaporated gas is liquefied.

Since the evaporated gas decompressed or expanded by the evaporated gas liquefier 80 is cooled by the evaporated gas supplied from the liquefied gas storage tank 10 and also cooled by the flash gas supplied from the gas-liquid separator 90 , Sufficient re-liquidation can be achieved. That is, this embodiment can utilize the cold heat of the flash gas, so that the re-liquefaction efficiency higher than that using the heat exchange between the evaporated gases can be obtained.

A gas-liquid separator 90 separates the gas from the evaporated gas that has been depressurized or expanded in the evaporative gas liquefier 80. In the gas-liquid separator 90, the evaporation gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas can be recovered as a flash gas to the evaporation gas heat exchanger 60.

Here, the evaporated gas supplied to the gas-liquid separator 90 may be cooled or decompressed in the evaporative gas liquefier 80 to be cooled. For example, in the evaporative gas compressor (50), the evaporation gas may be multi-stage pressurized to have a pressure of 200 bar to 400 bar, and the temperature may be around 45 degrees. The evaporated gas raised to a temperature of about 45 degrees is recovered by the evaporated gas heat exchanger 60 and heat-exchanged with the evaporated gas of about -100 degrees and about 150 degrees supplied from the liquefied gas storage tank 10, -95, and is supplied to the evaporation gas liquefier 80. At this time, in the evaporating gas liquefier 80, the evaporation gas is cooled by the reduced pressure and can have a pressure of about 3 bar and a temperature of about -150.2 degrees.

At this time, the evaporation gas has a temperature lower than the boiling point at 3 bar, so that at least a part can be liquefied and the remainder can be present as gaseous flash gas. In this case, the flash gas also has a state of about -150 degrees, and the flash gas of -150 degrees is supplied to the evaporation gas heat exchanger 60 in the gas-liquid separator 90 and can be used to cool the evaporation gas.

As described above, in this embodiment, the evaporation gas supplied to the gas-liquid separator 90 is sufficiently cooled by the evaporation gas and the flash gas in the evaporation gas heat exchanger 60 and then decompressed to 3 bar in the evaporation gas liquefier 80, So that the liquefaction efficiency of the evaporation gas can be improved.

In this embodiment, liquefied evaporated gas can be recovered in the liquefied gas storage tank 10, and the flash gas generated in the gas-liquid separator 90 can be recovered in the evaporative gas heat exchanger 60 to heat-exchange the evaporated gas .

Liquid separator 90 separates the vaporized gas into a liquid and a gas and the liquefied evaporated gas and the flash gas are respectively passed through the liquid recovery line 19 and the gas recovery line 17 to the liquefied gas storage tank 10, Gas heat exchanger (60).

The liquid recovery line 19 is connected from the gas-liquid separator 90 to the liquefied gas storage tank 10 to recover the vaporized liquid state to the liquefied gas storage tank 10 and the gas recovery line 17 is connected to the gas- 90 to the evaporation gas heat exchanger 60 to recover the flash gas to the evaporation gas heat exchanger 60 to heat exchange the evaporation gas.

In this embodiment, the evaporation gas generated in the liquefied gas storage tank 10 is pressurized by external heat penetration and supplied to the liquefied gas consumer 20 to prevent the evaporation gas from being discarded, , It is possible to maximize the liquefaction efficiency by further cooling the evaporation gas with the flash gas.

FIG. 7 is a conceptual diagram of a liquefied gas processing system according to a third embodiment of the present invention, and FIG. 8 is a graph showing power consumption for a flow rate of an evaporative gas compressor in a general liquefied gas processing system.

The liquefied gas processing system 4 will be described with reference to Fig. This embodiment is different from the second embodiment only in the mixer 70 and the flash gas recovery line 18A. The same reference numerals denote the same or corresponding components as those of the above-described embodiments, and a duplicate description thereof will be omitted.

X, X ', Y, Y', Z, and Z 'shown in FIG. 7 will be described in the fifth to twelfth embodiments described with reference to FIGS. 10 to 17. FIG.

In this embodiment, the flash gas supplied from the gas-liquid separator 90 and heat-exchanged in the evaporative gas heat exchanger 60 can be recovered without being discharged to the outside. At this time, the present embodiment may be provided with a flash gas recovery line 18A, and the flash gas recovery line 18A may be connected from the evaporation gas heat exchanger 60 to the mixer 70. [ Here, the flash gas recovery line 18A may be provided with a separate valve such as a three-way valve 18B or a check valve to discharge the flash gas to the outside. In this case, the flash gas may be supplied to a consumer, such as a gas combustion apparatus (GCU) (not shown), a boiler (not shown), an engine, etc., and burned.

That is, the flash gas that has cooled the evaporation gas in the evaporation gas heat exchanger 60 may be partially re-introduced into the evaporation gas heat exchanger 60 through the mixer 70, and the rest may be supplied to the boiler or the like. At this time, the valve 18B can control the recirculating flow rate of the flash gas flowing into the evaporative gas compressor 50 by adjusting the flow rate of the flash gas discharged to the outside.

As described above, in this embodiment, in addition to the evaporated gas supplied from the liquefied gas storage tank 10, the liquefied gas consumer 20 is driven through the flash gas separated from the gas-liquid separator 90 to generate power do.

The mixer 70 is provided upstream of the evaporation gas heat exchanger 60 on the evaporation gas supply line 16 and is supplied with the flash gas that is supplied from the liquefied gas storage tank 10 and is recovered in the gas- Can be introduced. The mixer (70) may be in the form of a pressure tank, which is space for storing the evaporating gas and the flash gas. Here, the evaporated gas and the flash gas mixed in the mixer 70 are supplied to the evaporative gas heat exchanger 50.

That is, the flash gas generated in the gas-liquid separator 90 may be recovered into the mixer 70 without discarding, and the evaporated gas and the flash gas may be pressurized through the evaporative gas compressor 50 and then supplied to the liquefied gas consumer 20 .

At this time, the flash gas supplied from the gas-liquid separator 90 may be cooled to -150.2 degrees by being decompressed or expanded by the evaporation gas liquefier 80 as mentioned above. The flash gas supplied from the flash gas and the liquefied gas storage tank The evaporated gas is mixed in the mixer 70 and flows into the evaporation gas heat exchanger 60. [

The evaporated gas recovered along the evaporated gas return line 16A branched from the evaporated gas compressor 50 and the liquefied gas consumer 20 and connected to the evaporated gas heat exchanger 60 is discharged from the evaporated gas heat exchanger 60 And can be cooled by heat exchange with the supplied evaporating gas and the flash gas supplied from the gas-liquid separator 90.

The evaporated gas discharged from the evaporated gas heat exchanger 60 and flowing into the evaporated gas liquefier 80 is cooled by the flash gas and decompressed by the evaporated gas liquefier 80 to a relatively lower temperature Can be cooled. More evaporative gas can be liquefied by the evaporative gas liquefier 80 and recovered to the liquefied gas storage tank 10 than when only heat exchange between the evaporative gases is realized.

Therefore, in this embodiment, the gaseous evaporative gas in the evaporated gas cooled through the evaporative gas liquefier 80 is separated into flash gas in the gas-liquid separator 90 and supplied to the evaporative gas heat exchanger 60, The liquefaction efficiency of the evaporation gas can be increased by lowering the temperature of the evaporation gas recovered from the compressor 50 to the evaporation gas heat exchanger 60 and the evaporation gas liquefier 80 sufficiently.

In this embodiment, not only the evaporated gas from the liquefied gas storage tank 10 but also the flash gas is mixed with the evaporated gas and flows into the evaporated gas compressor 50, so that a constant flow rate or more is supplied to the evaporated gas compressor 50 So that the driving efficiency can be improved.

As shown in the graph of FIG. 8, in the general evaporative gas compressor, when the flow rate is increased in the section B, the shaft power increases. This means that a large amount of power is required to compress the evaporated gas at a large flow rate. In this case, the section B may be a section having a larger flow rate than the predetermined value (reference value determining the section A and the section B) which is determined according to the specifications of the evaporative gas compressor and the driving conditions.

On the other hand, when the flow rate of the evaporative gas flowing into the evaporative gas compressor (50) is smaller than the predetermined value, the power consumption does not decrease even if the flow rate is decreased. This is because there is a risk of surging when a constant volume of evaporation gas is not introduced into the evaporation gas compressor 50. When the evaporation gas flow rate flowing into the evaporation gas compressor 50 is lower than a preset value, A part of the gas is recycled and the evaporated gas inlet volume of the evaporative gas compressor 50 must be maintained at a predetermined value or more, thereby causing power consumption for recycling.

However, since the evaporative gas compressor 50 of this embodiment can introduce the flash gas into the evaporative gas compressor 50 together with the evaporative gas, even if the flow rate of the evaporative gas decreases in the section A where the evaporative gas flow rate is lower than the predetermined value Since the volume required by the evaporative gas compressor (50) can be satisfied through the flash gas, power consumption can be reduced as the evaporative gas flow rate is reduced. That is, in the evaporative gas compressor 50 of the present embodiment, the power consumption can be proportionally reduced when the flow rate is reduced in the section A.

Therefore, in this embodiment, when the amount of the evaporation gas is small, the amount of the flash gas is controlled to reduce the recycle control of the evaporation gas compressor 50, and the power required for the low-load operation of the evaporation gas compressor 50 Can be saved.

In the evaporative gas compressor (50) of this embodiment, the power consumption increases as the flow rate increases in the section B. This is because a large amount of power is required to compress a larger amount of evaporation gas. However, since the present embodiment includes a configuration for circulating the flash gas, irrespective of the increase in the power consumption of the evaporative gas compressor 50 depending on the flow rate of the evaporative gas, the efficiency of re-liquefaction of the evaporative gas is greatly improved .

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

As shown in FIG. 9, the liquefied gas processing system 5 according to the fourth embodiment of the present invention can be supplemented with a flash gas bypass line 17A as compared with an embodiment. The same reference numerals denote the same or corresponding components as those of the other embodiments described above, and a duplicate description thereof will be omitted.

X, X ', Y, Y', Z, and Z 'shown in FIG. 9 will be described in the fifth to twelfth embodiments described with reference to FIGS. 10 to 17. FIG.

The flash gas bypass line 17A branches at the gas recovery line 17 so that at least a portion of the flash gas discharged from the gas-liquid separator 90 bypasses the evaporative gas heat exchanger 60. [ The bypassed flash gas flows into the mixer 70 along with the flash gas recovery line 18A in a low temperature state where no heat is supplied from the evaporation gas and is mixed with the evaporation gas or is supplied to the boiler (not shown), the gas combustion apparatus And can be discharged to a demand place such as an engine.

The flash gas heat exchanged with the evaporation gas in the evaporation gas heat exchanger 60 is heated to about 40 degrees by being supplied with heat while cooling the evaporation gas so that when the evaporation gas flows into the mixer 70 in a heated state, The temperature of the evaporation gas flowing into the evaporator 60 can be increased, which may lead to a decrease in the re-liquefaction efficiency.

Thus, the present embodiment can allow at least some of the flash gas to bypass the evaporative gas heat exchanger 60 and then mix with the evaporative gas in the mixer 70, at which time the temperature of the flash gas entering the mixer 70 By controlling the temperature of the evaporated gas in the liquefied gas storage tank 10 to be equal to or similar to the temperature of the evaporated gas, it is possible to prevent the re-liquefaction rate from being lowered due to the mixing of the flash gas cooled by the evaporated gas.

At this time, the bypass flow rate of the flash gas can be adjusted through the three-way valve 17B provided at the point where the flash gas bypass line 17A branches at the gas recovery line 17. Of course, the three-way valve 17B may be provided at a point where the flash gas bypass line 17A joins the flash gas recovery line 18A, and a check valve or the like may be provided on the flash gas bypass line 17A instead of the three- . ≪ / RTI >

Thus, in this embodiment, the present embodiment is characterized in that the evaporation gas generated in the liquefied gas storage tank 10 is pressurized and supplied to the liquefied gas consumer 20 by external heat penetration, or the flash gas is supplied to the evaporation gas compressor (50) and pressurized together with the evaporated gas to supply it to the liquefied gas consumer (20) to prevent the evaporated gas from being discarded, thereby saving the fuel. Further, the evaporation gas is further cooled by the flash gas, And by using the flash gas in combination with the evaporation gas, a constant flow rate or more is supplied to the evaporative gas compressor 50, thereby minimizing the recycle control and improving the driving efficiency.

FIG. 10 is a conceptual diagram of a liquefied gas processing system according to a fifth embodiment of the present invention, FIG. 11 is a conceptual diagram of a liquefied gas processing system according to a sixth embodiment of the present invention, Fig. 2 is a conceptual diagram of a liquefied gas processing system according to the present invention.

13 is a conceptual diagram of a liquefied gas processing system according to an eighth embodiment of the present invention, Fig. 14 is a conceptual diagram of a liquefied gas processing system according to a ninth embodiment of the present invention, Fig. 15 is a tenth embodiment Fig. 7 is a conceptual diagram of a liquefied gas processing system according to an example.

FIG. 16 is a conceptual diagram of a liquefied gas processing system according to an eleventh embodiment of the present invention, and FIG. 17 is a conceptual diagram of a liquefied gas processing system according to a twelfth embodiment of the present invention.

In the case of the fifth to twelfth embodiments of the present invention described with reference to FIGS. 10 to 17, only a partial view is shown in the drawing. In the process of describing the same, X, X ', Y, Y', Z and Z ' Except for the contents of heat exchange with each other, the configurations of the first to fourth embodiments described above can be applied equally or similarly, and the description is omitted.

In the following description of the embodiment of the present invention, the symbol X indicates that the evaporated gas discharged from the liquefied gas storage tank 10 is supplied to the evaporation gas heat exchanger 60 through the evaporation gas supply line 16, And X 'denote the inlet X and the outlet X' of the evaporator gas X 'supplied from the evaporative gas heat exchanger 60 to the evaporative gas compressor 50 by the evaporative gas supply line 16, . ≪ / RTI >

Y may denote a compressed evaporated gas inlet Y where the evaporated gas compressed by the evaporated gas compressor 50 returns to the evaporated gas heat exchanger 60 by the evaporated gas return line 16A , Y 'may refer to a compressed evaporated gas outlet (Y') supplied to the evaporative gas liquefier 80 in the evaporative gas heat exchanger 60 by the evaporative gas return line 16A.

The gas denoted by Z is compressed by the evaporative gas compressor 50 and then decompressed and liquefied through an evaporative gas liquefier (for example, a Rhodes Thompson valve) 80. Then, the gas separated by the gas-liquid separator 90 is returned to the gas recovery line Which is supplied to the evaporation gas heat exchanger 60 by means of the flash gas discharge line 18 or the flash gas discharge line 18A as indicated by Z ' And the flash gas outlet portion Z 'discharged from the evaporative gas heat exchanger 60.

The line connecting X and X ', Y and Y' or Z and Z 'may be a pipe and may be any type of supply means through which the fluid may flow. Hereinafter, the line may be expressed as X-X ', YY' or Z-Z '.

Referring to FIG. 10, the fifth embodiment includes two heat exchangers (first heat exchanger 60A and second heat exchanger 60B), and the first heat exchanger 60A comprises three streams, 2 is the same as the evaporation gas heat exchanger 60 mentioned in the embodiments and the like. That is, the compressed evaporated gas flowing along Y-Y 'in the first heat exchanger 60A can be cooled by the evaporating gas flowing along X-X' and the flash gas flowing along Z-Z ' .

Further, in the case of the second heat exchanger 60B, the compressed evaporative gas flowing along the line Y-Y 'is composed of two streams, and is supplied to the second heat exchanger 60B by the flash gas flowing along the line Z- Can be cooled. That is, the compressed evaporated gas flowing along the Y-Y 'is firstly cooled by the flash gas through the first heat exchanger 60A, and then the evaporated gas of X-X' in the first heat exchanger 60A and Can be secondarily cooled by the flash gas of Z-Z '.

Referring to Fig. 11, in the case of the sixth embodiment, two heat exchangers (first heat exchanger 60C and second heat exchanger 60D) are included. The first heat exchanger 60C is composed of two streams, and allows Y-Y 'and Z-Z' to exchange heat, and specifically, a compressed evaporation gas flowing along Y-Y 'flows along Z-Z' And is cooled by the flash gas.

The second heat exchanger 60D is composed of two streams and allows heat exchange between X-X 'and Y-Y', and compressed evaporation gas flowing along Y-Y 'by the evaporation gas flowing along X-X' Is cooled.

That is, the compressed evaporated gas flowing along the line Y-Y 'is first cooled by the evaporated gas discharged from the liquefied gas storage tank 10 along the line X-X', and is then supplied to the flash gas flowing along the line Z-Z 'Lt; / RTI >

Referring to Fig. 12, the seventh embodiment includes a first heat exchanger 60E similar to the sixth embodiment. However, the seventh embodiment includes a second heat exchanger 60F composed of three streams, and the second heat exchanger 60F is similar to or similar to the evaporative gas heat exchanger 60 mentioned in the fourth embodiment or the like.

At this time, the compressed evaporative gas flowing along the Y-Y 'is firstly cooled by the evaporative gas of X-X' and the flash gas of the Z-Z 'in the second heat exchanger 60F, and the refrigerant of the first heat exchanger 60E ) By the flash gas of Z-Z '.

Referring to Fig. 13, the eighth embodiment is similar to the sixth embodiment (the first heat exchanger 60C and the second heat exchanger 60D in Fig. 11 correspond to the first heat exchanger 60G ) And the second heat exchanger 60H.) The third heat exchanger 60I may further be provided.

That is, the evaporated gas of X-X ', in which the compressed evaporative gas flowing along Y-Y' is first cooled in the second heat exchanger 60H, is supplied to the first heat exchanger The flash gas of Z-Z ', which is secondarily cooled in the second heat exchanger 60G, and the third heat exchanger 60I.

Referring to Fig. 14, in the case of the ninth embodiment, as an improvement of the first embodiment, the flash gas is merged into the evaporative gas introduced into the evaporative gas heat exchanger 60. Fig. However, since the flash gas contains a large amount of nitrogen, the load of the evaporative gas compressor 50 can be increased when the evaporated gas into which the flash gas is combined flows into the evaporative gas compressor 50, The efficiency of the evaporative gas consumer 20 may be lowered as the nitrogen ratio in the evaporative gas supplied to the evaporator 20 increases.

Therefore, the ninth embodiment makes it possible to partially discharge the evaporated gas to which the flash gas has merged at the rear end of the evaporative gas heat exchanger 60. [ For this purpose, a vent line 61 may be provided in the evaporation gas line.

The vent line 61 is connected to a vent valve (not shown) which is controlled by receiving a nitrogen content in the evaporative gas flowing through X-X 'by a separate sensor (not shown) The opening degree can be controlled. At this time, the evaporation gas discharged along the vent line 61 may include not only nitrogen but also evaporation gas. However, since nitrogen is a large proportion due to the inflow of the flash gas, The gas can be discharged together with nitrogen. That is, even if the evaporation gas is discharged through the vent line 61, the loss of the evaporation gas is not large.

The opening of the vent line 61 can be controlled by the vent valve to match the evaporation gas flow rate requested by the liquefied gas consumer 20. For example, when the mixed flow rate of the evaporated gas and the flash gas discharged from the liquefied gas storage tank 10 is 100, and the flow rate demanded by the liquefied gas consumer 20 is 80, the vent valve can be controlled to 200,000 vent.

The vent line 61 may be connected to an engine (not shown), a turbine (not shown), a boiler (not shown), a liquefaction device (not shown), a GCU Which may enable efficient use of energy.

Accordingly, the present embodiment can prevent the flash gas from being circulated continuously and emit nitrogen to the outside, thereby increasing system efficiency. The vent line 61 is located at the rear end of the evaporative gas heat exchanger 60 because the flash gas is faded by cold heat so that all the cold heat is transferred to the compressed evaporative gas flowing along Y-Y ' to be.

Referring to Fig. 15, in the case of the tenth embodiment, as an improvement of the first embodiment, it further includes a nitrogen separator 62. Fig. As described in the ninth embodiment, since the flash gas may occupy a large specific gravity of nitrogen, the efficiency of the liquefied gas consumer 20 may be lowered by continuously circulating the flash gas by joining the flash gas.

Therefore, the present embodiment is characterized in that, when the flash gas combined vaporized gas is returned to the evaporative gas heat exchanger 60 through the evaporative gas heat exchanger 60 and the evaporative gas compressor 50 via Y-Y ' So that the nitrogen content can be removed by passing through the separator 62.

The nitrogen separator 62 may include a nitrogen discharge line (not shown), and nitrogen may be supplied to a nitrogen demand source (not shown) that requires nitrogen in the vessel (not shown) through the nitrogen discharge line Can supply.

The nitrogen separator 62 separates nitrogen using a membrane, and can supply it to a nitrogen generator (not shown) or a nitrogen demand source that requires nitrogen through a nitrogen discharge line. The nitrogen separator 62 can be used as the nitrogen separator 62 used in the embodiment of the present invention as long as nitrogen can be separated by techniques other than those described above.

Nitrogen in the ship can serve as a sealing function for various machines (not shown), or it can perform heat insulation of the cold or liquefied gas storage tank 10 of a refueling device (not shown) The above-described devices may be included. However, since the above-described operations can be used in ships for a variety of purposes, the nitrogen demand site requiring nitrogen is not limited to the above-described apparatuses.

Referring to Fig. 16, in the case of the eleventh embodiment, as an improvement of the sixth embodiment, the flash gas branch line 61a merging from Z-Z 'to X-X' can be provided. Thus, the flash gas that has cooled the compressed evaporative gas flowing along Y-Y 'in the first heat exchanger 60C flows at least partially through the flash gas branch line 61a to evaporate Gas and may be introduced into the second heat exchanger 60D.

Referring to Fig. 17, in the case of the twelfth embodiment, as an improvement of the sixth embodiment, it further includes the third heat exchanger 60J. The third heat exchanger 60J is a device in which the flash gas that has provided the cold heat to the compressed evaporative gas of Y-Y 'in the first heat exchanger 60C is discharged from the evaporative gas compressor 50 through Y-Y' It is possible to further provide cold heat to the compressed evaporated gas.

At this time, the compressed evaporated gas flowing along the line Y-Y 'is firstly cooled by the flash gas in the third heat exchanger 60J, and the evaporated gas of X-X' in the second heat exchanger 60D is secondarily Cooled, and can be thirdly cooled by the flash gas in the first heat exchanger 60C.

18 is a conceptual diagram of a liquefied gas processing system according to a thirteenth embodiment of the present invention.

In the case of the thirteenth embodiment of the present invention described with reference to FIG. 18, only a partial view is shown, and it may further include a liquefied gas supply pump 101 and a heating unit 102.

In the process of explaining the thirteenth embodiment of the present invention, the configuration of the first to twelfth embodiments described above or the conventional configuration other than the contents of the liquefied gas storage tank can be applied or the similar description will be omitted.

The liquefied gas supply pump 101 may be disposed on the upper surface or the upper side of the liquefied gas storage tank 10 outside the liquefied gas storage tank 10 and may be disposed in the liquefied gas storage tank 10).

The liquefied gas supply pump 101 may further include a liquefied gas supply pump supply line 25. [ The liquefied gas supply pump supply line 25 is provided with a liquefied gas supply pump supply valve (not shown) to adjust the opening of the liquefied gas supply pump supply line 25, It is possible to control the flow rate of the liquefied gas.

In the thirteenth embodiment of the present invention, the internal pressure of the liquefied gas storage tank 10 is raised by the gaseous liquefied gas supplied by the heating unit 102, which will be described later, The liquefied gas stored in the liquefied gas storage tank 10 by internal pressure is subjected to pressure.

The liquefied gas stored in the liquefied gas storage tank 10 can be introduced into the liquefied gas supply pump 101 naturally through the liquefied gas supply pump supply line 25 by the pressure, The net positive suction head (NPSH) value required by the present invention can be sufficiently satisfied. Therefore, the liquefied gas supply pump 101 does not need to suck liquefied gas from the liquefied gas storage tank 10 through a separate power source, and the liquefied gas supply pump 101 is also provided inside the liquefied gas storage tank 10 The NPSH value of the liquefied gas supply pump 101 can be satisfied even when the liquefied gas storage tank 10 is located outside or inside the liquefied gas storage tank 10 without being immersed in the liquefied gas.

Therefore, the liquefied gas supply pump 101 does not require an additional power source for sucking the liquefied gas from the liquefied gas storage tank 10, thereby reducing the energy consumption of the liquefied gas supply pump 101, Energy use may be possible.

Further, since the liquefied gas supply pump 101 does not necessarily need to be provided in a liquefied gas inside the liquefied gas storage tank 10, the installation position of the liquefied gas supply pump 101 can be flexibly changed, And it is possible to utilize efficient space.

Further, since the NPSH value of the liquefied gas supply pump 101 is sufficiently satisfied, the occurrence of cavitation in the liquefied gas supply pump 101 can be suppressed, and efficient driving can be achieved. As a result, the liquefied gas supply pump 101 can achieve an additional effect of improving the durability and saving the maintenance cost.

The liquefied gas supply pump 101 is located on the upper surface of the liquefied gas storage tank 10 outside the liquefied gas storage tank 10 and can be directly connected to the liquefied gas storage tank 10 and driven.

Therefore, in the thirteenth embodiment of the present invention, there is no need to connect the liquefied gas storage tank 10 and the liquefied gas supply pump 101, and a separate connection pipe (for example, an inter pipe) is unnecessary It is possible to reduce production cost and to reliably drive it, to have an effect of easy installation, maintenance and repair, and to obtain an additional effect of preventing boiling of liquefied gas due to heat loss to the outside have.

In addition, since the liquefied gas supply pump 101 can be installed outside the liquefied gas storage tank 10, it is very easy to install the liquefied gas storage tank 10 and the installation cost can be saved, Maintenance and maintenance of the battery 101 may be very advantageous.

The liquefied gas supply pump 101 may be a reciprocating or centrifugal pump, or may be a booster pump 31.

The heating unit 102 may be installed outside the liquefied gas storage tank 10 and may change the liquefied gas supplied from the liquefied gas storage tank 10 to a gaseous state using a heat source supplied from the outside. The heating unit 102 can also supply the gaseous liquefied gas to return to the liquefied gas storage tank 10 again.

The heating unit 102 may be a heater, and any device capable of heating the liquefied gas to a gaseous state may be possible. The heating unit 102 can be supplied with the liquefied gas by the storage tank-heating unit supply line 23 to be described later, and can be supplied with additional liquefied gas by the storage tank-heating unit return line 22 to be described later have. The heating unit 102 can also supply the gaseous liquefied gas to the liquefied gas storage tank 10 by a heating unit-storage tank supply line 24 to be described later.

In addition, the heating unit 102 may supply the gaseous liquefied gas to the liquefied gas storage tank 10 to increase the internal pressure of the liquefied gas storage tank 10. [ Accordingly, the liquefied gas stored in the liquefied gas storage tank 10 is subjected to pressure, and the liquefied gas under pressure is naturally introduced into the liquefied gas supply pump 101. [

At this time, the flow rate of the liquefied gas introduced into the liquefied gas supply pump 101 can sufficiently satisfy the net positive suction head (NPSH) required by the liquefied gas supply pump 101. That is, the heating unit 102 supplies the liquefied gas in the gaseous state to the liquefied gas storage tank 10 to increase the internal pressure of the liquefied gas storage tank 10 so that the liquefied gas in the liquefied gas storage tank 10 By sub-cooling, the NPSH value required by the liquefied gas supply pump 101 can be satisfied.

Specifically, in the thirteenth embodiment of the present invention, the heating unit 102 can supply the gaseous liquefied gas to the liquefied gas storage tank 10, thereby increasing the internal pressure of the liquefied gas storage tank 10 And the boiling point of the liquefied gas is increased. Therefore, the liquefied gas inside the liquefied gas storage tank 10 is increased in boiling point due to an increase in internal pressure of the liquefied gas storage tank 10, so that the liquefied gas inside the liquefied gas storage tank 10 can be sub-cooled or saturated .

That is, in the thirteenth embodiment of the present invention, the boiling point of the liquefied gas in the liquefied gas storage tank 10 due to the internal pressure of the liquefied gas storage tank 10 rises, and the liquefied gas supply pump 101, So that the NPSH value required by the liquefied gas supply pump 101 can be sufficiently satisfied.

Therefore, since the heating unit 102 can sufficiently satisfy the NPSH value of the liquefied gas supply pump 101, cavitation generation in the liquefied gas supply pump 101 can be suppressed. Thus, in the thirteenth embodiment of the present invention, the liquefied gas supply pump 101 can be efficiently driven, the durability can be improved, and the maintenance cost can be further reduced.

In the thirteenth embodiment of the present invention, a storage tank-heating unit return line 22, a storage tank-heating unit supply line 23, and a heating unit-storage tank supply line 24 may be further included.

The storage tank-heating unit return line 22 may be branched on the liquefied gas supply line 21 and connected to the heating unit 102 and may connect the liquefied gas supply pump 101 and the heating unit 102. The storage tank-heating unit return line 22 can supply additional liquefied gas when the liquefied gas is insufficient in the heating unit 102.

The storage tank-heating unit supply line 23 can connect the liquefied gas storage tank 10 and the heating unit 102. The storage tank-heating unit supply line 23 can supply liquefied gas to the heating unit 102 to cause the heating unit 102 to produce liquefied gas in a gaseous state.

The heating unit-storage tank supply line 24 can connect the heating unit 102 and the liquefied gas storage tank 10. The heating unit-storage tank supply line 24 supplies the gaseous liquefied gas produced in the heating unit 102 to the liquefied gas storage tank 10 so as to increase the internal pressure of the liquefied gas storage tank 10 .

It is within the scope of the present invention to select and combine at least one or more embodiments in the group consisting of the first to thirteenth embodiments. That is, the present invention is not limited to the first to thirteenth embodiments, and the present invention is also applicable to those derived from combinations of the embodiments.

1, 2, 3, 4, 5: liquefied gas processing system 10: liquefied gas storage tank
11: outer tank 12: inner tank
13: Insulation part 14: Support
15: Baffle 16: Evaporative gas supply line
16A: evaporation gas return line 17: gas recovery line
17A: flash gas bypass line 17B: three-way valve
18: flash gas discharge line 18A: flash gas discharge line
18B: three-way valve 19: liquid recovery line
20: Liquefied gas consumer 21: Liquefied gas supply line
22: storage tank - heating unit return line 23: storage tank - heating unit supply line
24: heating unit-storage tank supply line 25: liquefied gas supply pump supply line
26: forced carburetor 30: pump
31: boosting pump 32: high pressure pump
40: Liquefied gas heat exchanger 50: Evaporative gas compressor
51: compressor front-end heat exchanger 60: evaporative gas heat exchanger
60A, 60C, 60E and 60G: first heat exchanger
60B, 60D, 60F, 60H: the second heat exchanger
60I, 60J: third heat exchanger 61: vent line
61a: flash gas branch line 62: nitrogen separator
70: Mixer 80: Evaporative gas liquefier
90: gas-liquid separator 101: liquefied gas supply pump
102: Heating unit
A: The evaporation gas flow rate to the evaporation gas compressor is less than the predetermined value
B: the flow rate of the evaporating gas flowing into the evaporating gas compressor is larger than the preset value
X: Evaporating gas inlet X ': Evaporating gas outlet
Y: compressed evaporated gas inlet Y ': compressed evaporated gas outlet
Z: flash gas inlet Z ': flash gas outlet

Claims (10)

An evaporative gas compressor for compressing the evaporated gas supplied from the liquefied gas storage tank;
An evaporating gas liquefier for expanding or reducing the pressure of the evaporation gas compressed in the evaporation gas compressor to at least partially liquefy the evaporation gas;
A gas-liquid separator for separating a liquid and a gas from an evaporation gas passing through the evaporation gas liquefier;
A first heat exchanger formed in three streams for heat-exchanging the evaporated gas compressed in the evaporative gas compressor with the evaporated gas supplied from the liquefied gas storage tank and the gas supplied from the gas-liquid separator; And
And a second heat exchanger for exchanging heat between the evaporated gas compressed by the evaporative gas compressor and the gas supplied from the gas-liquid separator, the second heat exchanger being formed in two streams. The method of claim 1, wherein the evaporated gas compressed in the evaporative gas compressor
The first heat exchanger performs the first heat exchange with the evaporation gas supplied from the liquefied gas storage tank and the gas gas supplied from the gas-liquid separator,
And the second heat exchanger performs a second heat exchange with the gas gas supplied from the gas-liquid separator in the second heat exchanger. The method of claim 1, wherein the evaporated gas compressed in the evaporative gas compressor
Liquid separator, the first gas-liquid separator and the second gas-liquid separator,
Wherein the first heat exchanger performs secondary heat exchange with the evaporated gas supplied from the liquefied gas storage tank and the gas supplied from the gas-liquid separator. The gas-liquid separator according to claim 1, wherein the gas-
Wherein the first heat exchanger performs a first heat exchange with the compressed evaporated gas and the second heat exchanger performs a second heat exchange with the compressed evaporated gas. 3. The heat exchanger according to claim 2, wherein the gas-gas heat-exchanged in the second heat-
The liquefied gas is supplied to the engine, the turbine, the boiler, the liquefier or the GCU. 4. The heat exchanger according to claim 3, wherein the gas-gas heat-
The liquefied gas is supplied to the engine, the turbine, the boiler, the liquefier or the GCU. The method according to claim 1,
Further comprising a liquid recovery line connected to the liquefied gas storage tank in the gas-liquid separator to recover the liquid-state evaporated gas separated in the gas-liquid separator to the liquefied gas storage tank. The method according to claim 1,
Further comprising a mixer for mixing the vaporized gas supplied from the liquefied gas storage tank with the gas supplied from the gas-liquid separator. The method of claim 1, wherein the evaporating gas liquefier comprises:
Wherein the liquefied gas is an expander. The method of claim 1, wherein the evaporating gas liquefier comprises:
Lt; RTI ID = 0.0 > Thompson < / RTI > valve.

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