KR20160044103A - A Treatment System Of Liquefied Gas - Google Patents

Abstract

The present invention relates to a liquefied gas treatment system. The liquefied gas treatment system comprises: a boil-off gas supply line connected from a liquefied gas storage tank to a demand source; a boil-off gas compressor provided on the boil-off gas supply line and compressing boil-off gas; and a reliquefaction device storing the reliquefied boil-off gas by reliquefying the boil-off gas discharged from the boil-off gas compressor. Moreover, according to the present invention, the liquefied gas treatment system supplies liquefied gas at pressure required by the demand source is separated and stored in a liquid state through a phase separator in order to save system construction costs since a pump is unnecessary and sufficiently secure a system installation space.

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. The temperature and pressure necessary for driving the engine using such liquefied gas as fuel may be different from the state of the liquefied gas stored in the tank.

In addition, when LNG is stored in a liquid state, some LNG is vaporized and boil off gas (BOG) is generated as heat penetration occurs in the tank. Such evaporation gas may cause problems in a liquefied gas processing system. In order to solve the problem by discharging the evaporation gas to the outside (in the past, the evaporation gas was simply discharged to the outside in order to lower the tank pressure by lowering the tank pressure), the problem was solved. However, . Therefore, recently, as a technique for efficiently processing evaporative gas, there has been utilized a method of re-liquefying the generated evaporative gas and supplying it to the engine. However, since sufficient evaporative gas is not consumed even in such a utilization, efficient utilization And the ongoing research and development is being carried out.

It is an object of the present invention to provide a liquefied gas processing system for making the selectivity of the drive equipment flexible by making it possible to use a compressor available at room temperature through a preheater.

It is also an object of the present invention to provide a liquefied gas processing system for supplying fuel to a customer through a high-pressure remelting device so that a pump for supplying fuel can be omitted.

It is also an object of the present invention to provide a liquefied gas processing system for preventing an oil or an impurity from being mixed in a liquefied gas returning to a liquefied gas by providing an impurity separator inside the phase separator.

A liquefied gas processing system according to an embodiment of the present invention includes a vapor gas supply line connected from a liquefied gas storage tank to a customer site; An evaporative gas compressor provided on the evaporative gas supply line and compressing the evaporative gas; And a liquefaction device for re-liquefying and storing the evaporated gas discharged from the evaporative gas compressor, wherein the demander is supplied with the evaporation gas from the liquefaction device.

Specifically, the remapping device can supply 25 to 30 bar of evaporative gas to the customer.

Specifically, the remapping apparatus includes a remapping refrigerant apparatus for supplying a heat exchange medium; A re-liquefying heat exchanger for exchanging heat between the evaporated gas compressed in the evaporative gas compressor and the heat exchange medium; And a phase separator for separating the vaporized gas supplied from the redistribution heat exchanger into a liquid phase and a vapor phase.

Specifically, the phase separator may store liquid or gaseous vapor at a pressure of 25 to 30 bar.

Specifically, the apparatus may further include a preheater for preheating the evaporated gas discharged from the liquefied gas storage tank through the refrigerant supplied from the redistribution refrigerant apparatus.

Specifically, the apparatus may further include a heater provided between the demander and the refill liquefier on the evaporation gas supply line, for heating the evaporative gas discharged from the refill liquefier.

Specifically, the customer is a DFDE, a gas turbine, or a gas combustion apparatus (GCU), and the remanufacturing apparatus supplies a liquid-phase evaporation gas to the DFDE or the gas turbine, .

Specifically, a liquefied gas supply line for connecting the liquid-vaporizing gas storage tank and the liquefaction device; And a pump for supplying the liquefied gas stored in the liquefied gas storage tank to the liquefaction device.

Specifically, the liquefaction device can supply the liquefied gas from the liquefied gas storage tank when the evaporation gas generation amount is smaller than the evaporation gas required amount of the demanding customer.

Specifically, the evaporative gas compressor is a reciprocating compressor and can discharge compressed gas of 25 to 30 bar by blowing in a minus 10 degrees to minus 5 degrees.

Specifically, the apparatus further includes a blanket gas supply device for supplying a blanket gas to the phase separator, wherein when the internal pressure of the phase separator drops below a preset pressure The blanket gas can be supplied to the phase separator.

Specifically, the system may further include a liquefied gas return line connecting the phase separator and the liquefied gas storage tank to return the liquid fuel from the phase separator to the liquefied gas storage tank.

Specifically, there is provided a pressure regulating valve provided between the demander and the liquefaction device to regulate the pressure of the evaporative gas supplied to the demander to a pressure required by the demander, wherein the demander is a low- It is an injection engine and can generate power by being supplied with a pressure of 8 bar to 20 bar.

The liquefied gas processing system according to the present invention has an optional preheater capable of efficiently driving and can be provided with a compressor that can be used even at room temperature, so that the selectivity of the driving equipment can be made flexible and the system construction cost can be saved.

Further, the liquefied gas processing system according to the present invention is directly supplied to a customer through a phase separator for separating and storing liquefied gas at a pressure required by a customer, thereby saving the cost of constructing a system, There is an effect that sufficient installation space can be secured.

Further, the liquefied gas processing system according to the present invention has an effect that the impurity or oil is not contained in the liquefied gas returning to the liquefied gas storage tank with the impurity separator, thereby increasing the durability and stability of the storage tank.

1 is a conceptual diagram of a liquefied gas processing system according to an embodiment of the present invention.
2 is a conceptual diagram of a liquefied gas processing system according to another embodiment of the present invention.
3 is a conceptual diagram of the phase separator of the liquefied gas processing system according to 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 liquefied gas processing system according to an embodiment of the present invention.

1, a liquefied gas processing system 1 according to an embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporative gas compressor 30, a re-liquefier 40a, , And a preheater 50a.

Hereinafter, the LNG may be used to encompass not only a liquid state NG but also a NG state such as a supercritical state for the sake of convenience. The evaporation gas may include not only gaseous state evaporation gas but also liquefied evaporation gas Can be used as a meaning.

The liquefied gas storage tank (10) stores liquefied gas to be supplied to the customer (20). The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, at which time the liquefied gas storage tank 10 may have the form of a pressure tank.

The liquefied gas storage tank 10 includes an outer tank (not shown), an inner tank (not shown), and a heat insulating portion (not shown). The outer tank is a structure that forms the outer wall of the liquefied gas storage tank 10, and may be formed of steel, and may have a polygonal cross section.

The inner tank is provided inside the outer tank, and can be supported and supported inside the outer tank by a support (not shown). At this time, the support may be provided on the lower end of the inner tank, and may be provided on the side of the inner tank for suppressing lateral movement of the inner tank.

The inner tank can be made of stainless steel and can be designed to withstand pressures from 5 bar to 10 bar (6 bar, for example). The reason why the inner tank is designed to withstand such a constant pressure is that the inner pressure of the inner tank can be increased as the liquefied gas contained in the inner tank is evaporated and the evaporation gas is generated.

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

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

As described above, in this embodiment, the use of the pressure tank type liquefied gas storage tank 10 having a vacuum type heat insulating portion between the outer tanks and the inner tank makes it possible to minimize the generation of the evaporated gas, It is possible to prevent a problem such as breakage of the storage tank 10 from occurring.

A first evaporation gas supply line 11 for supplying a liquefied gas may be provided between the liquefied gas storage tank 10 and the customer 20 and the first evaporation gas supply line 11 A compressor 30 and a preheater 50 (preferably a first preheater 51) may be provided to supply the evaporation gas to the consumer 20.

At this time, a first evaporation gas supply valve (not shown) is provided in the first evaporation gas supply line 11 so that the supply amount of the evaporation gas can be adjusted according to the opening degree of the first evaporation gas supply valve.

In the embodiment of the present invention, the first evaporation gas supply line 11 may further include a second evaporation gas supply line 12 branched from a front end of the evaporation gas compressor 30 to be described later.

The second evaporation gas supply line 12 may be equipped with a preheater 50 (preferably a second preheater 52) and a second evaporation gas supply valve (not shown) The supply amount of the evaporation gas can be adjusted by controlling the opening degree.

The second evaporation gas supply line 12 may be branched between the liquefied gas storage tank 10 and the evaporative gas compressor 30 in the first evaporation gas supply line 11 and may be branched into the liquefied gas storage tank 10 A branch inlet may be provided in the near side and a branch outlet may be provided in the vicinity of the evaporative gas compressor 30. [

Further, in the embodiment of the present invention, the first evaporation gas supply line 11 may further include a liquefied gas return line 13 branching from the downstream end of the evaporative gas compressor 30. [

The liquefied gas return line 13 may include a re-liquefying heat exchanger 41a and a phase separator 42a to be described later. A liquefied gas return valve (not shown) may be provided to control the opening degree of the liquefied gas return valve The supply amount of the evaporation gas discharged from the evaporation gas compressor 30 or the liquid evaporation gas to be returned to the liquefied gas storage tank 10 from the phase separator 42a can be adjusted.

The customer 20 is driven through the liquefied gas supplied from the liquefied gas storage tank 10. That is, the consumer 20 needs liquefied gas and is driven using the raw material as the raw material. The consumer 20 may be an engine (not shown), a boiler (not shown), a GCU (not shown), and the like.

The customer 20 may be a heterogeneous fuel engine (not shown) and may generate power to drive the boiler and other devices. When the customer 20 is a heterogeneous fuel engine, liquefied gas or fuel oil can be selectively supplied without being mixed with liquefied gas and fuel oil. This is to prevent the mixture of two materials having different combustion temperatures from being mixed, thereby preventing the efficiency of the engine from deteriorating.

The customer 20 may be a low-speed two-stroke low-pressure gas injection engine and supplies thrust to a floating structure (not shown). The low-pressure two-stroke low-pressure gas injection engine is a device that is driven by a piston (not shown) inside the cylinder (not shown) by the combustion of liquefied gas, ) Is rotated, and a shaft (not shown) connected to the crankshaft can be rotated. Accordingly, when the low-speed two-stroke low-pressure gas injection engine is driven, the propeller (not shown) connected to the shaft rotates, so that the floating structure can be moved forward or backward.

 The low-speed two-stroke low-pressure gas injection engine in the embodiment of the present invention may be a 2s DF engine (XDF engine) developed by wartsila, and may be driven according to an Otto cycle.

That is, in the low-speed two-stroke low-pressure gas injection engine, the air-fuel mixture supplied to the cylinder is first compressed to the top dead center, and at the moment when ignition is performed by the pilot fuel from the outside at the compression top dead center, So that explosive power is generated. At this time, the air-fuel mixture mass ratio may be in the form of a Lean burn engine which may be in a lean state less than 14.7: 1.

In this case, HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil) is used as the ignition fuel, and the ratio of the ignition fuel to the high-pressure gas is about 1:99.

The low-speed two-stroke low-pressure gas injection engine is capable of generating power by supplying liquefied gas of 8 to 20 bar (preferably 10 bar), and the state of the liquefied gas to be supplied is changed according to the state required by the low- It can be different.

In a large-sized ship (not shown), thrust is generated through a MEGI engine (not shown). However, in the embodiment of the present invention, a low-speed two-stroke low-pressure gas injection engine is used as an engine for generating thrust of a floating structure Many benefits are created.

The MEGI engine requires a high pressure of about 200 bar to about 300 bar, which is necessary for driving the supply fuel, and requires a considerable amount of electric power to be consumed, which is about 210KW to about 220KW (about 215KW) for driving.

On the other hand, the low-speed two-stroke low-pressure gas injection engine has a consumption power for driving at a low pressure of 8 to 20 bar (preferably 10 bar) necessary for driving the supply fuel to about 13 KW to 17 KW (about 15 KW) There is an effect that a large amount of electric power can be reduced as compared with an engine.

Further, the MEGI engine has a problem that the gas supply system (not shown) accompanying the MEGI engine is very complicated and takes up a lot of space in order to generate the pressure required by the MEGI engine because the driving pressure is extremely high.

The low-speed two-stroke low-pressure gas injection engine is advantageous in that the fuel supply system is very simple and the space occupied by the low-pressure gas injection engine is low because the driving pressure is low.

The consumer 20 described above is, for example, an engine. The consumer 20 is not limited to this, and may be variously applied where the liquefied gas is needed.

That is, the customer 20 may be a gas turbine (not shown). The gas turbine can receive and consume the evaporative gas supplied from the liquefied gas storage tank 10, and the power generated by the gas turbine can be used to propel the propeller (not shown) Backward can be implemented.

Such a gas turbine can be driven by supplying a low-pressure evaporation gas.

The evaporation gas compressor (30) is provided on the first evaporation gas supply line (11) and compresses the evaporation gas. The evaporative gas compressor 30 compresses the evaporated gas discharged from the liquefied gas storage tank 10 at approximately 1 bar to 1.5 bar (preferably 1.03 bar) to approximately 20 to 35 bar (preferably 30 bar) 20) or the heat exchanger (40).

The evaporated gas discharged from the liquefied gas storage tank 10 is cryogenic at a temperature of minus 100 degrees Celsius to minus 90 degrees Celsius. When the evaporative gas is supplied to the evaporative gas compressor (30), there is a problem that when the compressor capable of being compressed at room temperature is used, the compressor may malfunction or be damaged in severe cases. Therefore, conventionally, a cryogenic evaporative gas compressor is used for compressing the cryogenic evaporation gas, but this is disadvantageous in that the cost is high and installation cost is excessively high.

Therefore, in the first embodiment of the present invention, the cost of the compressor is reduced by using the evaporative gas compressor 30 at room temperature, thereby reducing the construction cost of the liquefied gas processing system 1. In order to drive the evaporative gas compressor 30 at room temperature, a preheater 50 for changing the evaporating gas at a cryogenic temperature to room temperature is further provided.

The preheater 50 for realizing the above effect will be described later.

The evaporating gas compressor 30 may be a reciprocating type compressor, which has an effect of securing a sufficient installation space as compared with a centrifugal compressor. Compared to a centrifugal compressor for compressing high pressure, 35 bar), which is advantageous in that the power consumption is reduced.

A plurality of evaporative gas compressors 30 may be provided, and an evaporative gas cooler (not shown) may be provided between the evaporative gas compressors 30. When the evaporation gas is pressurized by the evaporation gas compressor 30, the temperature may also rise with the pressure increase. Therefore, in this embodiment, the evaporation gas cooler can be used to lower the temperature of the evaporation gas again.

The evaporative gas cooler may be installed in the same number as the evaporative gas compressor 30, and each evaporative gas cooler may be provided downstream of each evaporative gas compressor 30.

As the evaporation gas compressor 30 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, in the present embodiment, the evaporation gas compressor can be easily liquefied by increasing the pressure of the evaporation gas.

Of course, the pressurization of the evaporating gas is not only for re-liquefaction, but also for supplying to the usable engine at low pressure. In the embodiment of the present invention, the engine is driven by a low pressure rather than an engine driven only by a high pressure. Therefore, the evaporative gas compressor 30 can pressurize the evaporative gas at a low pressure, that is, have.

The re-liquefier 40a is provided on the liquefied gas return line 13 and re-liquefies the evaporated gas. Specifically, the re-liquefier 40a includes a re-liquefying heat exchanger 41a for exchanging heat between the evaporated gas compressed in the evaporating gas compressor 30 and the heat exchange medium, A phase separator 42a for separating the refrigerant gas into a liquid phase and a vapor phase, and a re-liquefied refrigerant device 43 for supplying a heat exchange medium for re-liquefaction by heat exchange with the evaporation gas.

The re-liquefier 40a can be operated when the amount of evaporative gas generated in the liquefied gas storage tank 10 is larger than the amount of evaporative gas required by the customer 20.

Here, the liquefaction heat exchanger 41a and the phase separator 42a are provided on the liquefied gas return line 13, and the liquefied refrigerant device 43 can be indirectly connected to the liquefaction heat exchanger 41a.

The re-liquefying heat exchanger 41a can receive the heat exchange medium from the re-liquefied refrigerant device 43. The cold heat of the heat exchange medium cools the evaporation gas and the heat of the evaporation gas heats the heat exchange medium, .

At this time, since the heat exchange medium is heated by receiving heat from the evaporation gas, the heat source is supplied from the evaporation gas. This heat exchange medium can be supplied to the first pre-heater 51, which will be described later, through the re-liquefied refrigerant device 43. [

The phase separator 42a can receive the evaporated gas re-liquefied or the evaporated gas in the gaseous phase that has not been re-liquefied from the liquefaction heat exchanger 41a and can separate it into vapor and liquid. At this time, the phase separator 42a can return the liquid-state re-liquefied evaporated gas to the liquefied gas storage tank 10 through the liquefied gas return line 13. [

The re-liquefying refrigerant system 43 can be indirectly connected to the liquefaction heat exchanger 41a and the first pre-heater 51. [ That is, the re-liquefying refrigerant device 43 is indirectly connected to the first pre-heater 51 through the first heat exchanging medium supply line 431 and is connected to the re-liquefying heat exchanger 41a through the second heat exchanging medium supply line 432, Lt; RTI ID = 0.0 > and / or < / RTI >

Here, the heat exchange medium may include a first heat exchange medium to be supplied to the first pre-heater 51 to be described later, or a second heat exchange medium to be supplied to the re-liquefying heat exchanger 41a. The first heat exchange medium may supply a heat source to the first pre-heater 51 through the heat exchange medium first supply line 431 and the second heat exchange medium may be supplied through the heat exchange medium second supply line 432 to the re-liquefying heat exchanger The cold heat can be supplied to the heat exchanger 41a.

The preheater 50a can preheat the evaporated gas discharged from the liquefied gas storage tank 10 and supply the preheated evaporated gas to the evaporated gas compressor 30. [ The preheater 50a may include a first preheater 51, a second preheater 52 and a control valve 53. [

The first preheater 51 is provided on the first evaporation gas supply line 11 and receives a heat source through a heat exchange medium supplied from a remelting device 40 to be described later. At this time, the first pre-heater 51 may be used prior to the second pre-heater 52, which will be described later.

The first preheater 51 receives the heat source through the first heat exchange medium supplied by the re-liquefied refrigerant device 43 when the re-liquefier 40 is operated, and the first heat exchange medium and the liquefied gas storage tank 10 To the evaporation gas discharged from the evaporator.

The first pre-heater 51 may be connected in parallel to the second pre-heater 52 to receive the selective supply of the evaporative gas according to the opening degree of the control valve 53 to be described later.

The second preheater 52 is provided on the second evaporation gas supply line 12 and can receive a heat source through a heat exchange medium supplied from seawater, fresh water or waste heat. At this time, the second preheater 52 can be used only when the refueling device 40 is not operating.

Here, the waste heat may be the waste heat generated by the customer (20) specifically the gas combustion unit (GCU) or the waste heat generated by the exhaust gas of the DFDE.

The second preheater 52 may include a seawater pump 61 and a seawater line 62 when driven by seawater. In other words, the second pre-heater 52 is connected to the sea water line 62 through which the seawater can be supplied by the sea water pump 61.

The second preheater 52 may preheat the evaporated gas by exchanging heat between the supplied seawater and the evaporated gas discharged from the liquefied gas storage tank 10.

Here, the first pre-heater 51 or the second pre-heater 52 may raise the temperature of the evaporated gas discharged from the liquefied gas storage tank 10 from -10 ° C to -5 ° C and the evaporated gas may be supplied to the evaporative gas compressor 30).

The control valve 53 is provided in a three-way valve structure at a point where the first evaporation gas supply line 11 and the second evaporation gas supply line 12 are connected to each other and the first evaporation gas supply line 11 or the second evaporation gas supply line 12, The supply of the evaporation gas to the supply line 12 can be controlled.

The control valve 53 supplies the evaporation gas discharged from the liquefied gas storage tank 10 to the first evaporation gas supply line 11 when the refueling device 40 is operated and the refueling device 40 is operated It is possible to supply the evaporated gas discharged from the liquefied gas storage tank 10 to the second evaporated gas supply line 12.

Concretely, when the remapping device 40 is operated, the control valve 53 is rich in the heat source generated in the remapping refrigerant device 43, so that the first preheater 51 (indirectly connected to the remapping refrigerant device 43) ) Can be preferentially used.

The control valve 53 closes the opening connected to the second evaporation gas supply line 12 and opens the opening connected to the first evaporation gas supply line 11 when the refueling device 40 is operated, It is possible to prevent the evaporation gas from being supplied to the gas supply line 12 and supply the evaporation gas to the first evaporation gas supply line 11.

When the re-liquefier 40 is not operated, the second pre-heater 52 connected to the other heat source may be used because the heat source generated in the re-liquefier refrigerant device 43 is insufficient.

The control valve 53 opens the opening connected to the second evaporation gas supply line 12 and closes the opening connected to the first evaporation gas supply line 11 to disconnect the first evaporation gas supply line 11, It is possible to prevent the evaporation gas from being supplied to the evaporation gas supply line 11 and to supply the evaporation gas to the second evaporation gas supply line 12. [

As a result, the evaporative gas compressor (30) at room temperature can be installed and used in the embodiment of the present invention, thereby reducing the installation cost. The heat source to be supplied to the preheater 50a can be selectively supplied using the waste heat of the refueling device 40 or the consumer 20 or seawater so that the selectivity of the preheater 50a can be made flexible.

As described above, the liquefied gas processing system 1 according to an embodiment of the present invention can include a compressor that can be used even at room temperature by providing an optional preheater capable of driving efficiently, so that the selectivity of the driving equipment becomes flexible, There is a saving effect.

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

2, the liquefied gas processing system 2 according to another embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporative gas compressor 30, a re-liquefier 40b, , And a preheater 50b. The configuration excluding the consumer 20, the liquefaction device 40b, and the preheater 50b in the other embodiment of the present invention is the same as the configuration in the liquefied gas processing system 1 according to the embodiment of the present invention, But not necessarily the same configuration.

In another embodiment of the present invention, the evaporation gas branch line 15 and the third evaporation gas supply line 16 may be further included.

The evaporation gas branch line 15 is branched at the downstream end of the evaporation gas compressor 30 and connected to the second customer site 22 to supply the evaporation gas. The third evaporation gas supply line 16 is connected to the phase separator 42b and the second customer site 22 to supply the evaporative gas.

At this time, an evaporation gas branching valve (not shown) or a third evaporation gas branching valve (not shown) is provided in the evaporation gas branch line 15 and the third evaporation gas supply line 16, Accordingly, the supply amount of the evaporation gas can be adjusted.

Further, in another embodiment of the present invention, the liquefied gas supply line 14 may be further included.

The liquefied gas supply line 14 can supply the liquefied gas stored in the liquefied gas storage tank 10 by connecting the liquefied gas storage tank 10 and the liquefaction unit 40b, And may be connected to a phase separator 42b to be described later.

The liquefied gas supply line 14 may be provided with a pump 141 and the pump 141 may be provided inside the liquefied gas storage tank 10 to supply the liquefied gas to the phase separator 42b.

At this time, the liquefied gas supply line 14 includes a liquefied gas supply valve (not shown) so that the supply amount of the liquefied gas can be adjusted according to the opening degree of the valve.

The consumer 20 may include a first consumer 21 and a second consumer 22. The first consumer 21 may be connected to the first evaporation gas supply line 11 to receive the evaporation gas and only the liquefied evaporated gas may be supplied through the re-liquefier 40b described later.

The first consumer 21 may be a DFDE or a gas turbine, and it may be supplied with liquefied evaporative gas only through the re-liquefier 40b.

The second customer 22 may be connected to the evaporation gas branch line 15 or the third evaporation gas supply line 16 to be supplied with the evaporation gas, 40b and can be supplied with the evaporated gas which is not liquefied in the phase separator 42b through the third evaporation gas supply line 16. [

Here, the second customer 22 may be a gas-fired unit (GCU). If the amount of evaporated gas required by the first customer 21 is larger than the amount of evaporated gas generated by the liquefied gas storage tank 10, It is possible to supply extra evaporation gas (the difference between the evaporation gas required amount of the first consumer 21 and the evaporation gas generation amount of the liquefied gas storage tank 10) in order to prevent an increase in internal pressure of the liquefied gas storage tank 10.

In addition, the customer 20 may have various configurations such as GCU, DFDE, MEGI, XDF (2sDF) engine and boiler.

The re-liquefier 40b re-liquefies the evaporated gas discharged from the evaporative gas compressor 30. At this time, the re-liquefier 40b can supply the liquefied evaporated gas to the customer 20.

The re-liquefier 40b can store the re-liquefied evaporation gas at 25 bar to 35 bar (preferably 30 bar), and can supply the stored re-liquefied vaporized gas to the customer 20 at a pressure condition of 25 bar to 35 bar without decompression have.

Specifically, the re-liquefier 40b includes a re-liquefying heat exchanger 41b for liquefying the evaporation gas compressed in the evaporating gas compressor 30 by heat exchange with the heat exchange medium, a re-liquefaction heat exchanger 41b for liquefying the evaporation gas supplied from the liquefaction heat exchanger 41b, A phase separator 42b for separating the refrigerant into a liquid phase and a vapor phase, and a re-liquefied refrigerant device 43 for supplying a heat exchange medium for heat exchange with the evaporation gas to re-liquefy.

The re-liquefying heat exchanger 41b is provided on the first evaporation gas supply line 11 and is provided with a heat exchange medium which is supplied from the re-liquefied refrigerant device 43 with evaporative gas of 25 bar to 35 bar discharged from the evaporative gas compressor 30 The evaporation gas can be liquefied by heat exchange.

The re-liquefying heat exchanger 41b is indirectly connected to the re-liquefied refrigerant device 43 and the second heat exchange medium supply line 432 to receive the heat exchange medium. At this time, the heat exchange medium supplied from the re-liquefied refrigerant device 43 can receive a heat source from the evaporated gas compressed from the evaporative gas compressor 30, and the evaporated gas compressed from the evaporative gas compressor 30 can be supplied to the re- The cold source can be supplied from the heat exchange medium supplied from the heat exchanger 43.

The phase separator 42b is provided on the first evaporation gas supply line 11 and can supply and store the re-liquefied evaporation gas from the re-liquefaction heat exchanger 41b. At this time, the phase separator 42b can store the re-liquefied evaporation gas of 25 bar to 35 bar (preferably 25 bar to 30 bar) without decompression and can directly supply the stored liquefied evaporation gas to the customer 20 without a separate pump have.

Therefore, in another embodiment of the present invention, the evaporator gas in the state of 25 bar to 35 bar is stored in the phase separator 42b without decompression and is supplied to the customer 20 in the above state as it is, The construction cost of the processing system 2 is saved, and the installation space of the liquefied gas processing system 2 can be easily secured.

The phase separator 42b can receive the liquefied gas from the liquefied gas storage tank 10 through the liquefied gas supply line 14 when the amount of evaporation gas generated is smaller than the required amount of liquefied gas in the customer 20, It is possible to supply the liquid vapor gas to the first consumer 21 in the consumer 20 in detail.

The phase separator 42b can supply the unevaporated vapor of the evaporative gas to the second customer 22 in the customer 20 in detail. The vaporized gas supply to the second customer 22 can be performed only in an emergency in which the internal pressure of the liquefied gas storage tank 10 rises.

The re-liquefying refrigerant device 43 may be indirectly connected to the pre-heater 50b through the heat exchange medium first supply line 431 and may be indirectly connected through the re-liquefying heat exchanger 41b and the heat exchange medium second supply line 432 Can be indirectly connected.

The heat exchange medium may include a first heat exchange medium supplied to the preheater 50b and a second heat exchange medium supplied to the liquefaction heat exchanger 41b.

In the embodiment of the present invention, a liquefied gas return line 13 may be further included.

The liquefied gas return line 13 can return the liquid fuel to the liquefied gas storage tank 10 by connecting the liquefied gas storage tank 10 and the phase separator 42b.

At this time, the liquefied gas return line 13 is provided with a liquefied gas return valve (not shown) so that the return amount of the liquefied gas can be adjusted in accordance with the opening degree of the liquefied gas return valve.

The preheater 50b can preheat the evaporated gas supplied from the liquefied gas storage tank 10 through the heat exchange medium supplied from the re-liquefied refrigerant device 43. [

The preheater 50b is provided between the liquefied gas storage tank 10 and the evaporative gas compressor 30 on the first evaporation gas supply line 11 and is connected to the re-liquefied refrigerant device 43 and the heat exchange medium first supply line 431 ). ≪ / RTI >

The preheater 50b exchanges the heat exchange medium supplied through the liquefied refrigerant device 43 and the evaporated gas discharged from the liquefied gas storage tank 10 when the refill liquor 40b operates, It is possible to supply the preheated vapor gas to the evaporator.

At this time, the evaporation gas may be preheated to a temperature of about minus 10 degrees Celsius to minus 5 degrees Celsius.

In the embodiment of the present invention, a heater 70 may be further included. The heater 70 is provided between the phase separator 42b and the consumer 20 on the first evaporation gas supply line 11 and supplies the liquefied evaporated gas discharged from the phase separator 42b to the demander 20 Lt; / RTI >

In an embodiment of the present invention, a blanket gas supply device 80 may be further included. The blanket gas supply device 80 is connected to the phase separator 42b and can supply the blanket gas to the phase separator 42b when the pressure of the phase separator 42b becomes lower than a preset pressure. Here, the predetermined pressure may be a pressure of 25 to 30 bar.

That is, when the phase separator 42b is below the preset pressure, the blanket gas supply device 80 supplies the blanket gas to the phase separator 42b so that the phase separator 42b can maintain the preset pressure So that the phase separator 42b can smoothly supply the fuel to the consumer 20.

The blanket gas supply device 80 may further include a blanket gas supply line 81 and may be connected to the phase separator 42b through the blanket gas supply line 81 and may be connected to the blanket gas supply line 81, It is possible to supply the blanket gas to the phase separator 42b.

As described above, the liquefied gas processing system 2 according to another embodiment of the present invention is a system for directly processing a liquefied gas directly to a customer 20 (20) through a phase separator 42b for separating and storing a liquefied gas at a pressure required by a customer 20 So that the pump 2 is unnecessary, so that the construction cost of the system 2 can be saved and the installation space for the system 2 can be sufficiently secured.

3 is a conceptual diagram of the phase separator of the liquefied gas processing system according to the present invention.

3, the phase separator 42 according to the embodiment of the present invention includes a housing 421 and an impurity separator 422. In the embodiment of the present invention, the first evaporation gas supply line 11, the liquefied gas return line 13, the liquefied gas supply line 14, and the like are provided in the liquefied gas processing system 1 according to the embodiment of the present invention, In the liquefied gas processing system 2 according to another embodiment of the present invention, the same reference numerals are used for the respective constructions and the like, but they are not necessarily referred to as the same constructions.

The housing 421 is formed with a space and surrounds the space.

The housing 421 may be formed of a material capable of withstanding a pressure of approximately 25 bar to 35 bar (preferably 30 bar) and may be supplemented with a stiffener to withstand such pressure.

The housing 421 can store liquid vapor or gaseous vapor, and can have a pressure vessel shape. It is also possible to store not only the evaporation gas but also the impurities (preferably oil) used in the evaporative gas compressor 30.

The housing 421 may have an inlet (not shown) for allowing evaporation gas or impurities to flow into the side surface, and may include an impurity separator 422 to be described later. The impurity separator 422 will be described in detail below.

The inlet may be provided on the upper side or the upper side of the phase separator 42 and may be supplied with the evaporation gas or liquefied gas or impurities through the first evaporation gas supply line 11 or the liquefied gas supply line 14. [

The housing 421 may have a discharge port (not shown) for discharging liquefied evaporative gas, and the discharge port includes a first discharge port and a second discharge port.

The first discharge port is provided on the upper side of the impurity separating device 422 to be described later to discharge the liquid evaporative gas present inside the housing 421 to the outside of the housing 421. Here, the first discharge port can supply the liquid evaporated gas to the liquefied gas storage tank 10 through the liquefied gas return line 13.

At this time, when liquid evaporation gas is supplied together with the impurities to the liquefied gas storage tank 10, wax may be formed in the liquefied gas storage tank 10 so that the driving of the liquefied gas processing systems 1 and 2 And can cause a fatal blow to the pipeline formed in the liquefied gas processing system 1, 2. In severe cases, the liquefied gas treatment system 1, 2 may be destroyed.

Therefore, in the embodiment of the present invention, the phase separator 42 is provided with the impurity separating device 422 to be described later so that no impurities are added to the liquefied gas storage tank 10. Therefore, the durability of the liquefied gas storage tank 10 can be improved to prolong the service life, and the driving reliability of the liquefied gas processing system 1, 2 can be improved.

Further, since the evaporative gas compressor (30) using oil can be provided, the selectivity of the constituent devices of the liquefied gas processing system (1, 2) can be made flexible and the evaporative gas can be compressed at a high pressure, There is an effect that can be anger.

The second discharge port is provided below the impurity separator 422 to discharge the evaporation gas or impurities in the liquid inside the housing 421 to the outside of the housing 421.

Here, the second discharge port can supply liquid vapor gas or impurities to the customer 20 through the first vapor gas supply line 11. [

That is, the storage material stored in the phase separator 42 is a mixture of liquefied evaporated gas and impurities. At this time, the impurities are precipitated at a high density and beneath the liquefied evaporated gas.

Therefore, the liquid-phase gas storage tank 10 is severely damaged when it contains impurities, so that the phase separator 42 separates the first discharge port from the first discharge port so that pure liquefied vapor gas is supplied to the liquefied gas storage tank 10 So that the impregnated impurities can be prevented from being supplied to the liquefied gas storage tank 10.

Since the engine or the like of the demander 20 does not cause much damage even if mixed with impurities, the phase separator 42 is provided with the second discharge port under the impurity separator 422 and the precipitated impurities are mixed with the consumer 20 You can enter it.

The impurity separator 422 is provided on one side of the housing 421 to separate impurities from the evaporated gas. Specifically, the impurity separation device 422 includes a fixing portion 4221, a filtering portion 4222, a rotating portion 4223, or a translating portion 4224.

The fixing portion 4221 may be connected to one side of the housing 421 to fix the impurity separating device 422 to the housing 421. [ The size of the fixing portion 4221 is not limited and can be freely configured if it is defined only within the area of the housing 421 of the phase separator 42. [

The filtering section 4222 can protrude from the fixing section 4221 toward the other side of the housing 421 facing the fixing section 4221. [ The filtering section 4222 may be integrally formed and connected to the rotating section 4223 to be described later and indirectly connected to the fixing section 4221 and may be deflected upward or downward from the fixing section 4221 by the rotating section 4223 (Not shown) for fixing the first folding portion (not shown) and the rotating portion 4223 and the fixing portion 4221. The second folding portion (not shown)

The rotating portion 4223 can rotate the filtering portion 4222 so as to be deflected upward or downward from the fixing portion 4221. [ The rotating portion 4223 can be provided between the filtering portion 4222 and the fixing portion 4221 to connect the filtering portion 4222 to the fixing portion 4221 together with the rotation of the filtering portion 4222, (Specifically, the rotating portion 4223 may be provided between the first filtering portion and the second filtering portion).

The translating portion 4224 is provided between the fixing portion 4221 and the filtering portion 4222 so that the filtering portion 4222 can be moved up and down. In this case, the translating portion 4224 may be formed in the form of a rail or in a sawtooth shape.

The translating portion 4224 can move the filtration portion 4222 upward or downward according to the level of the liquid evaporation gas stored in the phase separator 42 or depending on the position of the impurities to be precipitated.

Thus, the phase separator 42 according to the present invention is provided with the impurity separator 422 so that the liquefied gas returning to the liquefied gas storage tank 10 can be prevented from containing impurities or oil, ) Is increased in durability and stability.

Further, the driving reliability of the liquefied gas processing system (1, 2) is improved, and a compressor using oil can be used, so that the range of selection of the construction equipment can be widened and the compression range can be widened, Can be increased.

1,2: liquefied gas processing system 10: liquefied gas storage tank
11: first evaporation gas supply line 12: second evaporation gas supply line
13: liquefied gas return line 14: liquefied gas supply line
141: Pump 15: Evaporative gas branch line
16: Third evaporation gas supply line 20: Demand source
21: first customer 22: second customer
30: Evaporative gas compressor 40a, 40b: Re-liquefying device
41a, 41b: Liquefaction heat exchanger 42a, 42b:
421: housing 422: impurity separator
4221: fixing part 4222:
4223: rotating part 4224:
43: Re-liquefied refrigerant device 431: Heat exchange medium first supply line
432: Heat exchange medium second supply line 50a, 50b: Preheater
51: first preheater 52: second preheater
53: Control valve 61: Seawater pump
62: sea water line 70: heater
80: blanket gas supply device 81: blanket gas supply line

Claims (13)

An evaporative gas supply line connected from the liquefied gas storage tank to the customer;
An evaporative gas compressor provided on the evaporative gas supply line and compressing the evaporative gas; And
And a re-liquefying device for re-liquefying and storing the evaporated gas discharged from the evaporative gas compressor,
The above-
And the evaporation gas is supplied from the remelting device. 2. The liquefaction apparatus according to claim 1,
And the evaporation gas of 25 to 30 bar is supplied to the customer. 2. The liquefaction apparatus according to claim 1,
A re-liquefied refrigerant apparatus for supplying a heat exchange medium;
A re-liquefying heat exchanger for exchanging heat between the evaporated gas compressed in the evaporative gas compressor and the heat exchange medium; And
And a phase separator for separating the vaporized gas supplied from the redistribution heat exchanger into a liquid phase and a gaseous phase. The apparatus of claim 3, wherein the phase separator comprises:
Characterized in that the liquid or gaseous vapor is stored at a pressure of 25 to 30 bar. The method of claim 3,
Further comprising a preheater for preheating the evaporated gas discharged from the liquefied gas storage tank through the refrigerant supplied from the redistribution refrigerant apparatus. The method according to claim 1,
Further comprising a heater disposed on the evaporation gas supply line between the demander and the refill liquefier to heat evaporative gas discharged from the refill liquefier. 4. The system according to claim 3,
A DFDE, a gas turbine or a gas-fired unit (GCU)
The remelting device comprises:
The liquid vapor is fed to the DFDE or the gas turbine,
Wherein the vaporized gas is supplied to the gas combustion apparatus. The method according to claim 1,
A liquefied gas supply line for connecting the liquefied gas storage tank and the liquefaction device; And
Further comprising a pump for supplying the liquefied gas stored in the liquefied gas storage tank to the liquefaction device. 9. The liquefaction apparatus according to claim 8,
When the evaporation gas generation amount is smaller than the evaporation gas requirement amount of the customer,
And the liquefied gas is supplied from the liquefied gas storage tank. The compressor according to claim 1,
Wherein the reciprocating compressor compresses and discharges the evaporation gas entering from -10 ° C to -5 ° C at a pressure of 25 bar to 30 bar. The method of claim 3,
Further comprising a blanket gas supply device for supplying a blanket gas to the phase separator,
Wherein the blanket gas supply device comprises:
Wherein the blanket gas is supplied to the phase separator when the internal pressure of the phase separator drops below a predetermined pressure. The method of claim 3,
Further comprising a liquefied gas return line connecting the phase separator and the liquefied gas storage tank to return liquid fuel from the phase separator to the liquefied gas storage tank. The method according to claim 1,
And a pressure control valve provided between the customer and the liquefaction device for controlling the pressure of the evaporation gas supplied to the customer to a pressure required by the customer,
The above-
Low-pressure two-stroke gas injection engine and is supplied with a pressure of 8 to 20 bar to generate power.

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