KR20190006720A - Liquefaction system of gas and ship having the same - Google Patents

Abstract

The present invention relates to a reliquefaction system of gas and a ship having the same, including a liquefaction part liquefying evaporation gas by using mixed refrigerant. The liquefaction part includes: a mixed refrigerant compressor compressing mixed refrigerant; a reliquefaction device liquefying evaporation gas by exchanging heat with mixed refrigerant; a pressure reducing valve depressurizing compressed mixed refrigerant in the mixed refrigerant compressor and reentering the same to the reliquefaction device; and an inhalation unit inhaling liquefied mixed refrigerant decompressed in the pressure reducing valve and additionally depressurizing the liquefied mixed refrigerant which has been decompressed.

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a gas remelting system,

The present invention relates to a gas remelting system and a ship including the same.

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 the liquid phase, 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 the evaporation gas re-liquefaction system, (To discharge the evaporation gas to the outside in order to eliminate the risk of damage of the tank by lowering the tank pressure in the past) by consuming the evaporation gas to the outside, Causing a problem of waste.

SUMMARY OF THE INVENTION The present invention has been made in order to solve the problems of the prior art as described above, and it is an object of the present invention to maximize the re-liquefaction efficiency of a mixed refrigerant by using an ejector, reduce a load of a compressor, The present invention provides a gas remelting system that implements a flow of returning oil to prevent solidification due to heat exchange with evaporation gas and a vessel including the same.

The gas re-liquefaction system according to an embodiment of the present invention includes a liquefier for liquefying evaporative gas using a mixed refrigerant, the liquefier comprising: a mixed refrigerant compressor for compressing the mixed refrigerant; A re-liquidifier for exchanging the evaporated gas with the mixed refrigerant by heat exchange; A pressure reducing valve for decompressing the mixed refrigerant compressed in the mixed refrigerant compressor and re-introducing the mixed refrigerant into the re-liquidifier; And a suction unit for sucking the liquid mixed refrigerant discharged from the re-liquidator through the mixed refrigerant in the liquid phase decompressed by the pressure reducing valve, and further depressurizing the reduced refrigerant mixture.

Specifically, the mixed refrigerant compressor is a screw type that uses oil for sealing and lubrication. The mixed refrigerant after being compressed in the mixed refrigerant compressor and then heat-exchanged with at least a part of the evaporated gas in the re- And an oil separator for separating the oil.

Specifically, when the decompression valve is a first liquid-phase decompression valve, the re-liquidator includes: an evaporation gas flow path through which the evaporation gas flows; A reducing valve refrigerant passage through which the liquid mixed refrigerant decompressed by the first liquid pressure reducing valve flows; A gas refrigerant passage through which the gaseous mixed refrigerant separated by the oil separator flows; A liquid refrigerant flow path through which the liquid mixed refrigerant separated by the oil separator flows; And a compressed refrigerant passage through which the mixed refrigerant compressed in the mixed refrigerant compressor flows.

Specifically, the compressed refrigerant flow path is formed so as to face at least a part of the evaporation gas flow path in the re-liquidator, and then the re-liquidator and the oil separator are connected to each other, and the liquid refrigerant flow path is formed in the re- The oil separator and the re-liquidator may be connected to face at least a part of the evaporation gas flow path.

Specifically, a cooler for cooling the mixed refrigerant compressed in the mixed refrigerant compressor; A second liquid pressure reducing valve for reducing the liquid mixed refrigerant discharged from the oil separator; A receiver for temporarily storing mixed refrigerant to be supplied to the mixed refrigerant compressor; And a mixed refrigerant compressor for providing the mixed refrigerant compressor, the cooler, the first liquid pressure reducing valve, the re-liquidator, the suction unit, the second liquid pressure reducing valve, the oil separator and the receiver, And may further include a circulation line.

Specifically, the suction unit may supply liquid mixed refrigerant from the pressure reducing valve refrigerant passage, reduce the pressure of the liquid mixed refrigerant from the liquid refrigerant passage, and then supply the reduced refrigerant to the receiver.

Specifically, the suction unit is an ejector, and the re-liquidator may be a printing plate heat exchanger (PCHE).

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

The gas remelting system and the ship including the same according to the present invention maximize the re-liquefaction efficiency of the mixed refrigerant, reduce the load of the compressor, prevent the oil contained in the mixed refrigerant from being solidified by heat exchange with the low- .

1 is a conceptual view of a ship including a gas remelting system according to an embodiment of the present invention.
2 is a schematic view showing a first embodiment of a liquefaction section of a gas remelting system according to an embodiment of the present invention.
3 is a schematic view showing a second embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.
4 is a conceptual view showing a third embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.
5 is a conceptual view showing a fourth embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.
6 is a conceptual view of a fifth embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.
7 is a conceptual view showing a sixth embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.
8 is a seventh conceptional view of a liquefaction section of a gas remelting system according to an embodiment of the present invention.

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

Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. Hereinafter, the evaporation gas re-liquefaction system of the present invention will be described, and the present invention includes a system for evaporating gas re-liquefaction and a vessel having the evaporation gas re-liquefaction system.

Herein, the liquefied gas may be used to mean all gas fuels generally stored in a liquid state such as LNG or LPG, ethylene, ammonia, etc. Boiling-off gas (BOG) May mean forced vaporized liquefied gas. However, the evaporation gas may be used to include not only the evaporation gas in the gaseous state but also the liquefied evaporation gas.

Also in the following, the reduced pressure may be a state generated through expansion, and conversely, the expansion may be a state generated by the depressurization, so that the depressurization and the expansion can be used in combination with each other.

1 is a conceptual view of a ship including a gas remelting system according to an embodiment of the present invention.

1, a gas re-liquefaction system 1 according to an embodiment of the present invention includes a liquefied gas storage tank 10, a pump 20, a vaporizer 30, an evaporative gas compressor 40, 50) and a vaporized gas-liquid separator (60).

Here, a ship (not shown) provided with the gas remelting system 1 has a hull H composed of a forward portion (not shown), a stern portion (not shown), and an upper deck (not shown) And the propeller shaft S is propelled and operated by transmitting the power produced by the engine E of the engine room (not shown) disposed on the stern part to the propeller P and operating.

Hereinafter, a gas remelting system 1 according to an embodiment of the present invention will be described with reference to FIG.

The gas re-liquefaction system 1 according to the embodiment of the present invention is a system in which a liquefied gas in a liquid state is taken out from a liquefied gas storage tank 10 through a pump 20 and pressurized, ) Is used. At this time, the liquefied gas flows into the liquefied gas supply line (L1) and is supplied to the engine E from the liquefied gas storage tank (10).

The evaporated gas in the gaseous state generated in the liquefied gas storage tank 10 is compressed by the evaporated gas compressor 40 through the evaporated gas supply line L2 and then supplied to the engine 10 via the evaporated gas main supply line L2a. (E), or may be supplied to the liquefier 50 through the vapor gas supply line L2b.

Hereinafter, individual configurations for implementing the gas regeneration system 1 according to the embodiment of the present invention will be described in detail.

The liquefied gas storage tank 10 stores the liquefied gas to be supplied to the engine E. The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, in which the liquefied gas storage tank 10 is in the form of a pressure tank that stores the liquefied gas at a pressure of 1 bar to 10 bar (for example 1.03 bar) Lt; / RTI >

Here, the engine E may be a marine propulsion engine (or turbine) and does not limit high pressure, medium pressure, low pressure, and the like. For example, the engine E may be an ME-GI engine having a required pressure of 200 to 400 bar, an XDF engine having a required pressure of 15 to 50 bar, or a DFDE engine having a required pressure of about 10 bar or the like. Alternatively, the engine E disposed in the ship in FIG. 1, or an engine (or turbine) for various purposes provided on the land, but not limited thereto.

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

The pump 20 is provided on the liquefied gas supply line L1 and supplies the liquefied gas stored in the liquefied gas storage tank 10 to the vaporizer 30 either inside or outside the liquefied gas storage tank 10 .

Specifically, the pump 20 is disposed between the liquefied gas storage tank 10 and the vaporizer 30 on the liquefied gas supply line L1 to pressurize the liquefied gas stored in the liquefied gas storage tank 10, 30).

At this time, the pump 20 is constituted by a primary pump (booster pump) and a secondary pump (high-pressure pump) depending on the type of the engine E and can pressurize the liquefied gas in accordance with the pressure required by the engine E . Of course, the pump 20 can be constituted by only one primary pump (booster pump).

Here, the pump 20 pressurizes the liquefied gas discharged from the liquefied gas storage tank 10 so that the pressure and the temperature may be somewhat higher, and the pressurized liquefied gas may still be in a liquid state.

The pump 20 may be a submergible pump if it is provided inside the liquefied gas storage tank 10 and may be a pump of the liquefied gas stored in the liquefied gas storage tank 10 when the pump 20 is installed outside the liquefied gas storage tank 10. [ It may be provided at a position inside the hull H lower than the water level and may be a centrifugal pump.

The vaporizer 30 is provided on the liquefied gas supply line L 1 and can vaporize the liquefied gas discharged from the pump 20.

Specifically, the carburetor 30 is provided on the liquefied gas supply line L1 between the engine E and the pump 20 to vaporize the liquefied gas supplied from the pump 20 so that the engine E is in a desired state .

The vaporizer 30 can use various fruits such as Glycol Water, Sea Water, Steam, Propane, or engine exhaust gas as a heat source for vaporizing the cryogenic liquefied gas, The vaporized liquefied gas can be supplied to the engine E without pressure fluctuation.

The evaporative gas compressor (40) is provided on the evaporative gas supply line (L2) and can pressurize the evaporative gas generated in the liquefied gas storage tank (10).

The evaporation gas compressor 40 pressurizes the evaporation gas generated in the liquefied gas storage tank 10 and discharged at a pressure of about 1 bar and a pressure required by the engine E or a pressure required by the liquefier 50, It may be supplied to the engine E through the evaporation gas main supply line L2a or may be supplied to the liquefaction section 50 through the evaporation gas portion supply line L2b.

The plurality of evaporation gas compressors (40) can pressurize the evaporation gas at multiple stages. For example, the evaporation gas compressor 40 may include two to three pistons (not shown) to pressurize the evaporation gas from the second stage to the third stage. (Of course, depending on the type of the engine E, 40) may be changed, and in the case of MEGI, for example, it may be constructed in 4 to 5 stages.

Between each end of the evaporative gas compressor 40, an evaporative gas cooler (not shown) may be provided. When the evaporation gas is pressurized by the evaporation gas compressor 40, the temperature can also be raised in accordance with the pressure increase. Therefore, the present embodiment can lower the temperature of the evaporation gas again by using the evaporation gas cooler. The evaporative gas cooler may be installed at the same number of stages as the evaporator gas compressor 40, and each evaporative gas cooler may be provided downstream of each stage of the evaporative gas compressor 40.

The evaporated gas-liquid separator 60 may be provided downstream of the liquefier 50 on the evaporated-gas-portion feed line L2b and the evaporated gas at least partially liquefied by the liquefier 50 is separated into a gas and a liquid .

At this time, the evaporated gas in the gaseous state may be consumed in a flash gas, and the flash gas may be consumed in a separate consumer such as a gas combustion apparatus (not shown), a power generation engine (not shown), and the like. .

The liquid state evaporation gas may also be returned to the liquefied gas storage tank 10 as liquefied gas or may be supplied to the engine E. Of course, the treatment of the liquefied vaporized gas is not limited to the above.

The evaporation gas pressure reducing valve 61 may be provided between the liquefying portion 50 on the evaporating gas portion supplying line L2b and the evaporating gas liquid separator 60 and may be provided at least partially in the re-liquidator 51a It is possible to perform control such as depressurizing the pressure of the evaporating gas, and / or to control the flow rate of the evaporating gas.

The liquefier 50 uses the mixed refrigerant to liquefy the evaporated gas. Specifically, the liquefier 50 is provided on the evaporation gas supply line L2b to supply the compressed evaporation gas from the evaporation gas compressor 40 to heat exchange with the mixed refrigerant, And is supplied to the vaporized gas-liquid separator 60.

Here, the term 'mixed refrigerant' refers to an MR (Mixed Refinerant), which is a refrigerant mixed with methane, propane, nitrogen and the like and may be a material well known in the re-liquefaction field, The demand pressure (not shown), the type and size of the liquefied gas storage tank 10, and the like.

The liquefier 50 may have various embodiments. More specifically, the liquefier 50 will be described in detail with reference to FIGS. 2 to 8. FIG.

2 is a schematic view showing a first embodiment of a liquefaction section of a gas remelting system according to an embodiment of the present invention.

2, the liquefier 50a according to the first embodiment includes a re-liquidator 51a, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, an oil filter 55, (56a), a mixed refrigerant gas-liquid separator (57), and a mixed refrigerant circulation line (L3). The mixer 51a, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the oil filter 55, the suction unit 56a and the mixed refrigerant gas-liquid separator 57 are mixed May be connected by the refrigerant circulation line (L3), and the mixed refrigerant circulation line (L3) may circulate the mixed refrigerant.

Hereinafter, the liquefaction section 50a according to the first embodiment of the gas re-liquefaction system 1 according to the embodiment of the present invention will be described with reference to Fig.

The re-liquidator 51a is provided downstream of the evaporative gas compressor 40 on the evaporative gas portion feed line L2b to heat-exchange the evaporative gas with the mixed refrigerant to liquefy. The re-liquidator 51a may have a structure having four or more flow paths and may be, for example, a printing plate heat exchanger (PCHE).

Specifically, the re-liquidator 51a may have a structure in which the gaseous mixed refrigerant and the liquid mixed refrigerant separated by the mixed refrigerant gas-liquid separator 57 to be described later independently flow.

More specifically, the re-liquidator 51a includes an evaporative gas flow passage 511a through which the evaporative gas flows, a gas refrigerant passage 512a through which the gaseous mixed refrigerant separated by the mixed refrigerant gas-liquid separator 57 flows, A liquid refrigerant passage 513a through which the liquid mixed refrigerant separated by the separator 57 flows and a compressed refrigerant passage 514a through which the mixed refrigerant compressed by the mixed refrigerant compressor 53 flows.

The evaporated gas heat-exchanged by the mixed refrigerant in the re-liquidator 51a can be at least partially liquefied.

The receiver 52 may temporarily store the mixed refrigerant to be supplied to the mixed refrigerant compressor 53. [ At this time, the receiver 52 can prevent the pressure fluctuation of the mixed refrigerant to be supplied to the mixed refrigerant compressor 53, or can supplement the leaked mixed refrigerant.

The mixed refrigerant compressor (53) compresses the mixed refrigerant. At this time, the pressure of the mixed refrigerant compressed by the mixed refrigerant compressor (53) may correspond to the pressure of the evaporative gas compressed by the evaporative gas compressor (40), and may be, for example, 30 to 50 bar.

The mixed refrigerant compressor (53) may be a screw type using oil for sealing and lubrication. Therefore, there is less concern about leakage of the mixed refrigerant by the mixed refrigerant compressor (53). In this case, although the present invention is equipped with the receiver 52, it is not necessary to provide a separate tank for supplementing the mixed refrigerant.

The mixed refrigerant compressor 53 may have at least one screw (not shown), and the screw can compress the mixed refrigerant while rotating around a rotating shaft (not shown) by a motor (not shown) . At this time, if there are a plurality of screws, the screws may be provided in multiple stages.

The mixed refrigerant compressor (53) uses oil for sealing and lubrication, so that oil can be mixed into the mixed refrigerant compressed by the screw. However, when the refrigerant mixture containing oil is heat-exchanged with the evaporation gas at a very low temperature, the oil may be solidified due to the cold heat of the evaporation gas, resulting in lower heat exchange efficiency or damage to the composition. In order to solve this problem, in the embodiment of the present invention, the oil filter 55 is disposed downstream of the mixed refrigerant compressor 53 to remove oil.

The cooler 54 is provided downstream of the mixed refrigerant compressor 53 and can cool the mixed refrigerant compressed in the mixed refrigerant compressor 53. Since the mixed refrigerant can be heated by receiving the compressed heat during compression similarly to the evaporative gas compressor 40 as described above, the present invention is characterized in that the cooler 54 is provided between the mixed refrigerant compressor 53 and the re- The temperature of the refrigerant can be lowered.

The mixed refrigerant flowing into the mixed refrigerant compressor (53) may be mixed with oil. At this time, the cooler 54 can cool the mixed refrigerant and transfer it to the re-liquidator 51a so that the oil has a complete liquid phase. At this time, an oil filter 55 is provided between the cooler 54 and the re-liquidator 51a By separating the liquid oil, the inflow of oil into the re-liquidator 51a can be blocked.

The suction unit 56a sucks the mixed refrigerant heat-exchanged in the re-liquidator 51a through the mixed refrigerant compressed in the mixed refrigerant compressor 53 and reduces the mixed refrigerant compressed in the mixed refrigerant compressor 53. [

Concretely, the suction unit 56a receives the compressed mixed refrigerant from the compressed refrigerant passage 514a, sucks the liquid mixed refrigerant from the liquid refrigerant passage 513a, decompresses it, and supplies it to the mixed refrigerant gas-liquid separator 57 . That is, the compressed mixed refrigerant supplied from the compressed refrigerant passage 514a is used as a driving fluid for the suction unit 56a, and the liquid mixed refrigerant supplied from the liquid refrigerant passage 513a flows through the suction fluid of the suction unit 56a And the driving fluid and the suction fluid may be mixed in the suction unit 56a and discharged to the mixed refrigerant gas-liquid separator 57. [ At this time, the driving fluid may be a gas and the suction fluid may be a liquid, so that the suction unit 56a can be driven by two phases.

The suction unit 56a has an advantage of maximizing the cooling effect as compared with a general pressure reducing valve because it can have a large heat and cold section in the interval of the pressure and the enthalpy property.

Here, the suction unit 56a may be, for example, an ejector.

The mixed refrigerant gas-liquid separator 57 is capable of gas-liquid separation of the mixed refrigerant discharged from the suction unit 56a.

The gaseous mixed refrigerant separated in the mixed refrigerant gas-liquid separator 57 can be introduced into the gas refrigerant passage 512a of the re-liquidator 51a, and the separated liquid refrigerant is supplied to the liquid refrigerant passage 513a.

At this time, the mixed refrigerant gas-liquid separator 57 can cause the oil not filtered by the oil filter 55 to be precipitated. Accordingly, the mixed refrigerant gas-liquid separator 57 can prevent the supply of oil to the re-liquidator 51a, thereby eliminating the risk of system shut-down due to solidification of the oil.

In the liquefied portion 50a, the mixed refrigerant circulates in the mixed refrigerant circulation line L3 to which the components are connected.

Specifically, the mixed refrigerant is supplied to the compressor 52 via the compressor 52, the mixed refrigerant compressor 53, the cooler 54, the oil filter 55, the compressed refrigerant passage 514a of the re-liquidator 51a, the suction unit 56a, Liquid separator 57, and then separated into a gas and a liquid in the mixed refrigerant gas-liquid separator 57. The mixed refrigerant of the gas flows into the gas refrigerant passage 512a of the re-liquidator 51a and flows into the receiver 52. The mixed refrigerant of the liquid flows into the liquid refrigerant passage 513a of the re-liquidator 51a, Unit 56a.

As described above, in the embodiment of the present invention, the suction unit 56a having a large cold-heat interval in the interval of the pressure and the enthalpy physical property is disposed in the liquefying unit 50a, The cooling effect is maximized, and the malfunction is less and the system reliability is improved.

3 is a schematic view showing a second embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.

3, the liquefier 50b according to the second embodiment includes a re-liquidator 51b, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, a suction unit 56a, A gas-liquid separator 57, an oil separator 58, a pressure reducing valve 63 and a mixed refrigerant circulation line L3. The refrigerant is supplied to the gas-liquid separator 57 through the re-liquidator 51b, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the suction unit 56a, the mixed refrigerant gas-liquid separator 57, The valve 63 can be connected by the mixed refrigerant circulation line L3 and the mixed refrigerant circulating line L3 can circulate the mixed refrigerant.

The liquefying portion 50b according to the second embodiment is different from the liquefaction portion 50a according to the first embodiment except that the oil filter 55 is omitted and the oil separator 58 and the pressure reducing valve 63 are added, The flow path structure of the firebox 51b is changed. Therefore, the configuration of the liquefier 50b according to the second embodiment other than the oil separator 58, the pressure reducing valve 63, and the re-liquidator 51b is the same as that of the liquefier 50a according to the first embodiment The same reference numerals can be used for the sake of convenience, but they are not necessarily referring to the same constituent elements.

Hereinafter, a liquefier 50b according to a second embodiment of the gas remelting system 1 according to the embodiment of the present invention will be described with reference to FIG.

However, as described above, there is a difference between the configuration of the liquefier 50a, the oil separator 58, the pressure reducing valve 63, and the re-liquidator 51b according to the first embodiment. ), The pressure reducing valve 63, and the re-liquidator 51b will be described in detail with reference to the remainder of the configuration as described for the liquefier 50a according to the first embodiment shown in FIG.

The re-liquidator 51b is provided downstream of the evaporative gas compressor 40 on the evaporative gas portion supply line L2b to heat-exchange the evaporative gas with the mixed refrigerant to liquefy it. The re-liquidator 51b is provided in a structure having five or more flow paths and may be, for example, a printing plate heat exchanger (PCHE).

Specifically, the re-liquidator 51b may have a structure in which the gas-phase mixed refrigerant separated by the mixed refrigerant gas-liquid separator 57 and the liquid-phase mixed refrigerant flow independently, and may be separated (separated) by an oil separator 58 The mixed refrigerant of the gaseous phase and the liquid mixed refrigerant may flow independently.

More specifically, the re-liquidator 51b includes an evaporative gas flow passage 511b through which the evaporative gas flows, a first gas refrigerant passage 512b through which the gaseous mixed refrigerant separated by the mixed refrigerant gas-liquid separator 57 flows, A first liquid coolant passage 513b through which the liquid mixed refrigerant separated by the refrigerant gas-liquid separator 57 flows, a compressed refrigerant passage 514b through which the mixed refrigerant compressed by the mixed refrigerant compressor 53 flows, an oil separator A second gas refrigerant passage 515b through which the gaseous mixed refrigerant separated by the oil separator 58 flows and a second liquid refrigerant passage 516b through which the liquid mixed refrigerant separated by the oil separator 58 flows .

The mixed refrigerant flowing into the mixed refrigerant compressor (53) may be mixed with oil. At this time, the cooler 54 can cool the mixed refrigerant and deliver it to the re-liquidator 51b so that the oil has a complete liquid phase. However, when the refrigerant mixture containing oil is heat-exchanged with the evaporation gas at a cryogenic temperature, the oil may coagulate due to the cold heat of the evaporation gas, resulting in lower heat exchange efficiency or damage to the composition.

However, in the liquefier 50b according to the second embodiment of the present invention, the mixed refrigerant in which the oil is mixed instead of the oil filter 55 (shown in Fig. 1) is not completely heat-exchanged with the evaporated gas in the re- By structuring at least a part of the heat exchange, it is possible to prevent the oil from solidifying.

The compressed refrigerant flow path 514b of the re-liquidator 51b is formed so as to face at least a part of the evaporation gas flow path 511b in the re-liquidator 51b and then the re-liquidator 51b and the oil separator 58 are connected And the second liquid refrigerant passage 516b may be formed so that the oil separator 58 and the first gas refrigerant passage 512b are connected so as to be at least partially shared with the first gas refrigerant passage 512b .

At this time, the compressed refrigerant passage 514b may be connected to the oil separator 58 by the mixed refrigerant circulation line L3 formed through the middle portion of the re-liquidator 51b, and the second liquid refrigerant passage 516b, Is connected to the intermediate portion of the re-liquidator 51b and the intermediate portion of the re-liquidator 51b by the mixed refrigerant circulation line L3 formed to be connected to the substantially middle portion of the first gas refrigerant passage 512b, A separator 58 may be connected.

The evaporated gas heat-exchanged by the mixed refrigerant in the re-liquidator 51a can be at least partially liquefied.

The oil separator 58 can separate the oil by gas-liquid separation of the mixed refrigerant heat-exchanged with at least a part of the evaporated gas in the re-liquidator 51b after being compressed in the mixed refrigerant compressor 53. [

As described in the re-liquidator 51b, the liquefier 50b according to the second embodiment of the present invention is configured such that the mixed refrigerant in which the oil is mixed is not completely heat-exchanged with the evaporated gas in the re-liquidator 51b, So as to prevent the oil from solidifying.

The oil separator 58 is connected to the compressed refrigerant passage 514b formed in the re-liquidator 51b so as to face at least a part of the evaporative gas passage 511b, Refrigerant is supplied and gas-liquid separation is performed.

At this time, since the separated gaseous phase does not contain oil, it is supplied to the re-liquidator 51b again to be able to exchange heat completely with mixed refrigerant flowing in the evaporation gas or other flow path. Since the separated liquid phase contains oil, when it is supplied to the re-liquidator 51b again, it is also possible to perform heat exchange with at least a part of the evaporated gas or the mixed refrigerant flowing in the other flow path.

As described above, the liquefied portion 50b of the second embodiment of the present invention is configured such that the mixed refrigerant in which the oil is mixed instead of the oil filter is heat exchanged at least in part in the re-liquidator 51b without completely exchanging heat with the evaporated gas, It is possible to reduce the construction cost and improve the reliability and durability of the re-liquidator 51b.

The pressure reducing valve 63 can depressurize the liquid mixed refrigerant separated in the oil separator 58 and supply the depressurized mixed refrigerant to the second liquid coolant passage 516b of the re-liquidator 51b again. At this time, the pressure reducing valve 63 may be referred to as a liquid pressure reducing valve.

In the liquefied portion 50b, the mixed refrigerant circulates in the mixed refrigerant circulation line L3 to which the components are connected.

Specifically, the mixed refrigerant flows in the order of the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the compressed refrigerant passage 514b of the re-liquidator 51b, and the oil separator 58, 58). ≪ / RTI > Liquid mixed refrigerant flows into the second liquid refrigerant passage 516b of the re-liquidator 51b and is mixed with the first gas refrigerant passage 512b and flows together with the mixed refrigerant in the first gas refrigerant passage 512b, Mixed refrigerant flows into the second gas refrigerant passage 515b of the re-liquidator 51b and flows into the suction unit 56b.

The mixed refrigerant flowing into the suction unit 56b flows into the mixed refrigerant gas-liquid separator 57 and is separated into gas and liquid in the mixed refrigerant gas-liquid separator 57. [ The gaseous mixed refrigerant flows into the first gas refrigerant passage 512b of the re-liquidator 51b to be mixed with the liquid mixed refrigerant separated by the oil separator 58 described above and flows into the receiver 52, Liquid mixed refrigerant flows into the first liquid coolant passage 513b of the re-liquidator 51b and flows into the suction unit 56a again.

As described above, in the embodiment of the present invention, the suction unit 56a having a large cold-temperature section in the interval of the pressure and the enthalpy physical property is disposed in the liquefying unit 50b, The cooling effect is maximized, and the malfunction is less and the system reliability is improved.

In the embodiment of the present invention, the refrigerant mixture in which the oil is mixed instead of the oil filter is configured to heat exchange at least part of the refrigerant in the re-liquidator 51b without completely exchanging heat with the evaporator gas, The construction cost is reduced and the reliability and durability of the re-liquidator 51b are improved.

4 is a conceptual view showing a third embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.

4, the liquefier 50c according to the third embodiment includes a re-liquidator 51c, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, an oil filter 55, (56b), a pressure reducing valve (62a), and a mixed refrigerant circulation line (L3). In this case, the re-liquidator 51c, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the oil filter 55, the suction unit 56b, and the pressure reducing valve 62a, Line L3, and the mixed refrigerant circulation line L3 can circulate the mixed refrigerant.

The liquefier 50c according to the third embodiment is different from the liquefier 50a according to the first embodiment except that the mixed refrigerant gas-liquid separator 57 is removed, a pressure reducing valve 62a is added, And the suction unit 56b are changed. Therefore, in the liquefaction unit 50c according to the third embodiment, the configurations other than the pressure reducing valve 62a, the re-liquidator 51c, and the suction unit 56b are the same as those in the liquefier 50a according to the first embodiment The same reference numerals can be used for the sake of convenience, but they are not necessarily referring to the same constituent elements.

Hereinafter, the liquefier 50c according to the third embodiment of the gas remelting system 1 according to the embodiment of the present invention will be described with reference to FIG.

However, as described above, there is a difference in the configuration of the liquefier 50a, the pressure reducing valve 62a, the re-liquidator 51c, and the suction unit 56b according to the first embodiment, and hence the pressure reducing valve 62a ), The re-liquidator 51c and the suction unit 56b will be described in detail, but the remaining configuration is the same as that described in the liquefier 50a according to the first embodiment shown in Fig.

The re-liquidator 51c is provided downstream of the evaporation gas compressor 40 on the evaporation gas portion supply line L2b to heat-exchange the evaporation gas with the mixed refrigerant to liquefy it. The re-liquidator 51c may have a structure having four or more flow paths and may be, for example, a printing plate heat exchanger (PCHE).

Concretely, the re-liquidator 51c may have a structure in which the mixed refrigerant decompressed by the pressure reducing valve 62a and the mixed refrigerant discharged by the suction unit 56b independently flow.

More specifically, the re-liquidator 51c includes an evaporation gas flow path 511c through which the evaporation gas flows, a suction unit refrigerant flow path 512c through which the mixed refrigerant discharged by the suction unit 56b flows, And a compressed refrigerant passage 514c through which the mixed refrigerant compressed by the mixed refrigerant compressor 53 flows.

The mixed refrigerant flowing into the mixed refrigerant compressor (53) may be mixed with oil. At this time, the cooler 54 can cool the mixed refrigerant and deliver it to the re-liquidator 51b so that the oil has a complete liquid phase. However, when the mixed refrigerant in which the oil is mixed is heat-exchanged with the evaporation gas at a very low temperature, the oil coagulates due to the cold heat of the evaporation gas, resulting in lower heat exchange efficiency or damage to the composition. The liquefying portion 50c can prevent the oil from solidifying by further constructing the oil filter 55. [

The evaporated gas heat-exchanged by the mixed refrigerant in the re-liquidator 51c can be at least partially liquefied.

The suction unit 56b sucks the mixed refrigerant heat-exchanged in the re-liquidator 51c through the mixed refrigerant compressed in the mixed refrigerant compressor 53 and reduces the mixed refrigerant compressed in the mixed refrigerant compressor 53. [ At this time, the suction unit 56c may be provided in parallel on the pressure reducing valve 62a and the mixed refrigerant circulation line L3.

Concretely, the suction unit 56b receives the gaseous compressed mixed refrigerant from the compressed refrigerant passage 514c of the re-liquidator 51c, sucks the liquid refrigerant from the reduced pressure refrigerant passage 513c, The refrigerant can be supplied to the suction unit refrigerant passage 512c of the re-liquidator 51c.

That is, the compressed mixed refrigerant supplied from the compressed refrigerant passage 514c is used as the driving fluid for the suction unit 56b, and the liquid mixed refrigerant supplied from the reduced pressure valve refrigerant passage 513c is sucked by the suction unit 56b And the driving fluid and the suction fluid may be mixed in the suction unit 56b and discharged to the suction unit refrigerant passage 512c of the re-liquidator 51c. At this time, the driving fluid may be a gas and the suction fluid may be a liquid, so that the suction unit 56b can be driven by two phases.

The suction unit 56b can have a large cold / warm section in the interval of the pressure and the enthalpy property, thereby maximizing the cooling effect compared with the pressure reducing valve 62a.

Here, the suction unit 56b may be, for example, an ejector.

The pressure reducing valve 62a decompresses the mixed refrigerant compressed by the mixed refrigerant compressor 53 and flows into the re-liquidator 51c. At this time, the pressure reducing valve 62a may be referred to as a vapor pressure reducing valve. Specifically, the pressure reducing valve 62a can heat the mixed refrigerant compressed in the mixed refrigerant compressor 53 by heat exchange in the re-liquidator 51c, and can supply the reduced refrigerant to the suction unit 56b and the mixed refrigerant circulating line L3 As shown in FIG.

More specifically, the pressure reducing valve 62a receives the gaseous compressed mixed refrigerant from the compressed refrigerant passage 514c of the re-liquidator 51c, decompresses it, and then supplies it to the reduced pressure valve refrigerant passage 513c of the remanufacturer 51c. .

As described above, in the liquefier 50c of the third embodiment of the present invention, since the suction unit 56b and the pressure reducing valve 62a are constructed in parallel with each other, the cooling effect of the mixed refrigerant is further raised, The use of the suction unit 56b having a high rate or the use of the decompression valve 62a having a low cooling rate can be selected to maximize the re-liquefaction rate of the evaporated gas.

In the liquefier 50c, the mixed refrigerant circulates in the mixed refrigerant circulation line L3 to which the components are connected.

Specifically, the mixed refrigerant flows in the order of the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the oil filter 55, and the compressed refrigerant passage 514c of the re-liquidator 51c, ) Or the suction unit 56b. The mixed refrigerant decompressed by the pressure reducing valve 62a flows into the pressure reducing valve refrigerant passage 513c of the re-liquidator 51c and flows into the suction unit 56b. The mixed refrigerant discharged from the suction unit 56b flows into the suction unit refrigerant passage 512c of the re-liquidator 51c and flows into the receiver 52. [

As described above, in the embodiment of the present invention, the suction unit 56b, which can have a large cold-heat interval in the interval of the pressure and the enthalpy property, is disposed in the liquefying unit 50c, The cooling effect is maximized, and the malfunction is less and the system reliability is improved.

In addition, in the embodiment of the present invention, the suction unit 56b and the pressure reducing valve 62a are provided in parallel to select the cooling rate of the mixed refrigerant according to the re-liquefaction rate of the evaporated gas, have.

5 is a conceptual view showing a fourth embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.

5, the liquefier 50d according to the fourth embodiment includes a re-liquidator 51d, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, a suction unit 56b, An oil separator 58, a pressure reducing valve 63, and a mixed refrigerant circulation line L3. In this case, the re-liquidator 51d, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the suction unit 56b, the pressure reducing valve 62a, the oil separator 58, 63 can be connected by the mixed refrigerant circulation line L3 and the mixed refrigerant can circulate in the mixed refrigerant circulation line L3 and the pressure reducing valve 62a is a gas phase pressure reducing valve and the pressure reducing valve 63 is liquid phase pressure reducing Valve. ≪ / RTI >

In the liquefier 50d according to the fourth embodiment, the oil filter 55 is removed from the liquefier 50c according to the third embodiment, the oil separator 58 and the pressure reducing valve 63 are added, The flow path structure of the fire machine 51d is changed. Therefore, the configuration of the liquefier 50d according to the fourth embodiment other than the oil separator 58, the pressure reducing valve 63, and the re-liquidator 51d is the same as that of the liquefier 50c according to the third embodiment The same reference numerals can be used for the sake of convenience, but they are not necessarily referring to the same constituent elements.

Hereinafter, the liquefaction section 50d according to the fourth embodiment of the gas remelting system 1 according to the embodiment of the present invention will be described with reference to FIG.

However, as described above, there is a difference in the configuration of the liquefier 50c, the oil separator 58, the pressure reducing valve 63, and the re-liquidator 51d according to the third embodiment. ), The pressure reducing valve 63, and the re-liquidator 51d will be described in detail, but the remaining configuration is the same as that described in the liquefier 50c according to the third embodiment shown in FIG.

The re-liquidator 51d is provided downstream of the evaporative gas compressor 40 on the evaporative gas portion supply line L2b to heat-exchange the evaporative gas with the mixed refrigerant to liquefy it. The re-liquidator 51d may have a structure having five or more flow paths and may be, for example, a printing plate heat exchanger (PCHE).

Specifically, the re-liquidator 51d may have a structure in which the gaseous mixture refrigerant decompressed by the gas-phase pressure reducing valve 62a and the liquid-phase mixed refrigerant decompressed by the suction unit 56b independently flow, The gas-phase mixed refrigerant separated by the oil separator 58 and the liquid-phase mixed refrigerant may flow independently.

More specifically, the re-liquidator 51d includes an evaporation gas flow path 511d through which the evaporation gas flows, a decompression valve refrigerant flow path 512d through which the gaseous mixed refrigerant decompressed by the gaseous pressure reducing valve 62a flows, A compressed refrigerant passage 514d through which the mixed refrigerant compressed by the mixed refrigerant compressor 53 flows, and a refrigerant passage 514d through which the mixed refrigerant is decompressed by the oil separator 58, A gas refrigerant passage 515d through which the mixed refrigerant flows and a liquid refrigerant passage 516d through which the liquid mixed refrigerant separated by the oil separator 58 flows.

The mixed refrigerant flowing into the mixed refrigerant compressor (53) may be mixed with oil. At this time, the cooler 54 can cool the mixed refrigerant and deliver it to the re-liquidator 51d so that the oil has a complete liquid phase. However, when the refrigerant mixture containing oil is heat-exchanged with the evaporation gas at a cryogenic temperature, the oil may coagulate due to the cold heat of the evaporation gas, resulting in lower heat exchange efficiency or damage to the composition.

However, in the liquefier 50d according to the fourth embodiment of the present invention, the mixed refrigerant in which the oil is mixed instead of the oil filter 55 (shown in Fig. 4) is not completely heat-exchanged with the evaporated gas in the re- By structuring at least a part of the heat exchange, it is possible to prevent the oil from solidifying.

To this end, the compressed refrigerant flow path 514d of the re-liquidator 51d is formed so as to face at least part of the evaporation gas flow path 511d in the re-liquidator 51d, and then the re-liquidator 51d and the oil separator 58 are connected And the liquid refrigerant passage 516d may be formed so that the oil separator 58 and the suction unit refrigerant passage 512d are connected so as to be at least partially shared with the suction unit refrigerant passage 512d.

At this time, the compressed refrigerant flow path 514d may be connected to the oil separator 58 by the mixed refrigerant circulating line L3, which is formed to penetrate only the middle portion of the re-liquidator 51d, and the liquid refrigerant flow path 516d, The intermediate portion of the re-liquidator 51d and the oil separator 58 are connected by the mixed refrigerant circulation line L3 which is drawn substantially in the middle portion of the re-liquidator 51d and connected to the substantially middle portion of the gas refrigerant passage 512d, Lt; / RTI >

The evaporated gas heat-exchanged by the mixed refrigerant in the re-liquidator 51d can be at least partially liquefied.

The oil separator 58 can separate the oil by gas-liquid separation of the mixed refrigerant heat-exchanged with at least a part of the evaporated gas in the re-liquidator 51d after being compressed by the mixed refrigerant compressor 53. [

As described in the re-liquidator 51d, the liquefied portion 50d according to the fourth embodiment of the present invention is configured such that the mixed refrigerant in which the oil is mixed is not completely heat-exchanged with the evaporated gas in the re-liquidator 51d, So as to prevent the oil from solidifying.

The oil separator 58 is formed so as to be connected to the compressed refrigerant passage 514d formed in the re-liquidator 51d so as to face at least a part of the evaporative gas passage 511d so that the compressed mixture Refrigerant is supplied and gas-liquid separation is performed.

At this time, since the separated gaseous phase contains no oil, it is supplied to the re-liquidator 51d again to be able to exchange heat completely with the mixed refrigerant flowing in the evaporation gas or other flow path. Since the separated liquid phase contains oil, when it is supplied to the re-liquidator 51d again, it can also perform heat exchange with at least a part of the evaporated gas or mixed refrigerant flowing in the other flow path.

Thus, the liquefied portion 50d of the fourth embodiment of the present invention is configured such that the mixed refrigerant in which the oil is mixed instead of the oil filter is heat exchanged at least in part in the re-liquidator 51d without being completely heat-exchanged with the evaporated gas, It is possible to reduce the construction cost and improve the reliability and durability of the re-liquidator 51d.

The liquid pressure reducing valve 63 can depressurize the liquid mixed refrigerant separated by the oil separator 58 and supply the reduced mixed refrigerant to the liquid refrigerant passage 516d of the re-liquidator 51d again.

The mixed refrigerant in the liquefied portion 50d circulates in the mixed refrigerant circulation line L3 to which the components are connected.

Specifically, the mixed refrigerant flows in the order of the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the compressed refrigerant passage 514d of the re-liquidator 51d, and the oil separator 58, 58). ≪ / RTI > Liquid mixed refrigerant flows into the liquid refrigerant passage 516d of the re-liquidator 51d and is mixed with the gas refrigerant passage 512d and flows together with the mixed refrigerant in the gas refrigerant passage 512d, Is introduced into the gas refrigerant passage 515d of the evaporator 51d and supplied in parallel to the suction unit 56b or the vapor reduction valve 62a.

The mixed refrigerant flowing into the suction unit 56b is supplied to the suction unit refrigerant passage 512d of the re-liquidator 51d and flows into the receiver 52. The mixed refrigerant introduced into the vapor pressure reducing valve 62a is supplied to the re- 51d to the decompression valve refrigerant passage 512d and supplied to the suction unit 56b.

As described above, in the embodiment of the present invention, the suction unit 56b, which can have a large cold-heat interval in the interval of the pressure and the enthalpy property, is disposed in the liquefying unit 50d, The cooling effect is maximized, and the malfunction is less and the system reliability is improved.

Further, in the embodiment of the present invention, the refrigerant mixed with oil instead of the oil filter is configured to heat exchange at least part of the refrigerant in the re-liquidator 51d without completely exchanging heat with the evaporated gas, thereby preventing the oil from solidifying The construction cost is reduced and the reliability and durability of the re-liquidator 51d are improved.

6 is a conceptual view of a fifth embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.

6, the liquefier 50e according to the fifth embodiment includes a re-liquidator 51e, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, a suction unit 56c, An oil separator 58, a pressure reducing valve 63, and a mixed refrigerant circulation line L3. In this case, the re-liquidator 51e, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the suction unit 56c, the pressure reducing valve 62b, the oil separator 58, 63 can be connected by the mixed refrigerant circulation line L3 and the mixed refrigerant can circulate in the mixed refrigerant circulation line L3 and the pressure reducing valve 62b is connected to the first liquid pressure reducing valve and the pressure reducing valve 63 And may be referred to as a second liquid pressure reducing valve.

The liquefying portion 50e according to the fifth embodiment differs from the arrangement of the suction unit 56c in the liquefier 50d according to the fourth embodiment and the arrangement of the re-liquidator 51e and the flow path structure of the first liquid pressure reducing valve 62b Was changed. Therefore, in the liquefier 50e according to the fifth embodiment, the configuration other than the suction unit 56c, the re-liquidator 51e and the first liquid pressure reducing valve 62b is the same as that of the liquefier 50d according to the fourth embodiment The same reference numerals can be used for the respective configurations and convenience, but the same configurations are not necessarily referred to.

Hereinafter, the liquefier 50e according to the fifth embodiment of the gas remelting system 1 according to the embodiment of the present invention will be described with reference to FIG.

However, as described above, since there is a difference in the configuration of the re-liquidator 51e, the suction unit 56c and the first liquid-phase pressure reducing valve 62b with respect to the liquefier 50d according to the fourth embodiment, The configuration of the re-liquidator 51e, the suction unit 56c and the first liquid pressure reducing valve 62b will be described in detail, but the remaining configuration is the same as that of the liquefier 50d according to the fourth embodiment shown in Fig. 5 I am in the bar.

The re-liquidator 51e is provided downstream of the evaporation gas compressor 40 on the evaporation gas portion supply line L2b to heat-exchange the evaporation gas with the mixed refrigerant to liquefy it. The re-liquidator 51e may have a structure having five or more flow paths and may be, for example, a printing plate heat exchanger (PCHE).

Concretely, the re-liquidator 51e is configured so that the liquid mixed refrigerant decompressed by the first liquid pressure reducing valve 62b and the gaseous mixed refrigerant separated by the oil separator 58, which will be described later, . ≪ / RTI >

More specifically, the re-liquidator 51e includes an evaporation gas flow path 511e through which the evaporation gas flows, a pressure reducing valve refrigerant flow path 512e through which liquid mixed refrigerant depressurized by the first liquid pressure reducing valve 62b flows, A compressed refrigerant passage 513e through which the mixed refrigerant compressed in the refrigerant compressor 53 flows, a gas refrigerant passage 514e through which the gaseous mixed refrigerant separated by the oil separator 58 flows, And a liquid refrigerant passage 515e through which the liquid mixed refrigerant separated by the refrigerant flows.

The mixed refrigerant flowing into the mixed refrigerant compressor (53) may be mixed with oil. At this time, the cooler 54 can cool the mixed refrigerant and transfer it to the re-liquidator 51e so that the oil has a complete liquid phase. However, when the refrigerant mixture containing oil is heat-exchanged with the evaporation gas at a cryogenic temperature, the oil may coagulate due to the cold heat of the evaporation gas, resulting in lower heat exchange efficiency or damage to the composition.

However, the liquefied portion 50e according to the fifth embodiment of the present invention is configured such that the mixed refrigerant in which the oil is mixed instead of the oil filter 55 (shown in Fig. 2 or Fig. 4) It is possible to prevent the solidification of the oil by configuring the heat exchanging at least part of the heat exchange.

To this end, the compressed refrigerant passage 513e of the re-liquidator 51e is formed to face at least part of the evaporative gas passage 511e in the re-liquidator 51e, and then the re-liquidator 51e and the oil separator 58 are connected And the liquid refrigerant passage 515e may be connected to the re-liquidator 51e and the oil separator 58 so that the liquid refrigerant passage 515e is formed so as to face at least part of the evaporative gas passage 511e in the re-liquidator 51e.

At this time, the compressed refrigerant passage 513e may be connected to the oil separator 58 by the mixed refrigerant circulation line L3 formed through the middle portion of the re-liquidator 51e only, and the liquid refrigerant passage 515e may be connected to the oil separator 58, Is connected to the mixed refrigerant circulation line (L3) through the intermediate portion of the re-liquidator (51e) so that the intermediate portion of the re-liquidator (51d) and the oil separator (58) can be connected.

The evaporated gas heat-exchanged by the mixed refrigerant in the re-liquidator 51e can be at least partially liquefied.

The first liquid pressure reducing valve 62b decompresses the mixed refrigerant compressed in the mixed refrigerant compressor 53 and re-flows it into the re-liquidator 51e.

Specifically, the first liquid pressure reducing valve 62b can be depressurized by receiving the mixed refrigerant compressed in the mixed refrigerant compressor 53 and heat-exchanged in the re-liquidator 51e, and the reduced mixed refrigerant is supplied to the re- To the pressure reducing valve refrigerant passage 512e.

The suction unit 56c sucks the liquid mixed refrigerant discharged from the re-liquidator 51e through the liquid mixed refrigerant depressurized by the first liquid pressure reducing valve 62b to further reduce the pressure of the liquid refrigerant in the depressurized state .

Concretely, the suction unit 56c receives the mixed refrigerant depressurized from the pressure reducing valve refrigerant passage 512e, sucks the liquid mixed refrigerant from the liquid refrigerant passage 515e, and reduces the pressure, and then supplies the reduced refrigerant to the receiver 52 . That is, the compressed mixed refrigerant supplied from the pressure reducing valve refrigerant passage 512e is used as a driving fluid for the suction unit 56c, and the liquid mixed refrigerant supplied from the liquid refrigerant passage 515a is sucked by the suction unit 56c And the driving fluid and the suction fluid may be mixed in the suction unit 56c and discharged to the receiver 52. [ At this time, both the driving fluid and the suction fluid may be liquid, so that the suction unit 56c can be driven by a single phase (1phase).

The suction unit 56c has an advantage that the cooling effect is maximized as compared with a general pressure reducing valve because it can have a large heat and cold section in the interval of the pressure and the enthalpy property.

In addition, the suction unit 56c of the present invention has an effect of increasing the boosting effect as compared with suction units driven by a single phase and driven by another phase, thereby reducing the power consumption of the mixed refrigerant compressor 53. [

Here, the suction unit 56c may be, for example, an ejector.

In the liquefied portion 50e, the mixed refrigerant circulates in the mixed refrigerant circulation line L3 to which the components are connected.

Specifically, the mixed refrigerant flows in the order of the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the compressed refrigerant passage 514e of the re-liquidator 51e, and the oil separator 58, 58). ≪ / RTI > The mixed refrigerant of the separated liquid flows into the liquid refrigerant passage 515e of the re-liquidator 51e and is sucked into the suction unit 56c. The mixed refrigerant of the separated gas flows into the gas refrigerant passage 514e And is supplied to the first liquid pressure reducing valve 62b.

The mixed refrigerant introduced into the suction unit 56b is directly supplied to the receiver 52. The mixed refrigerant introduced into the first liquid pressure reducing valve 62b is supplied to the reduced pressure valve refrigerant passage 512e of the re- And is supplied to the suction unit 56c.

As described above, in the embodiment of the present invention, the suction unit 56c, which can have a large cold / warm section in the interval of the pressure and the enthalpy property, is disposed in the liquefied portion 50e, In addition, the suction unit 56c according to the present invention has a higher step-up effect than the suction units driven by a single phase and driven by another phase, It is possible to reduce the power consumption of the power unit 53.

7 is a conceptual view showing a sixth embodiment of the liquefaction section of the gas remelting system according to the embodiment of the present invention.

7, the liquefier 50f according to the sixth embodiment includes a re-liquidator 51f, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, a suction unit 56d, An oil separator 58, a pressure reducing valve 63, and a mixed refrigerant circulation line L3. In this case, the re-liquidator 51f, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the suction unit 56d, the pressure reducing valve 62b, the oil separator 58, 63 can be connected by the mixed refrigerant circulation line L3 and the mixed refrigerant can circulate in the mixed refrigerant circulation line L3 while the pressure reducing valve 62b is connected to the first pressure reducing valve and the pressure reducing valve 63 is connected to the 2 pressure reducing valve.

The liquefaction section 50f according to the sixth embodiment has the arrangement of the suction unit 56d in the liquefaction section 50e according to the fifth embodiment and the flow path structure of the re-liquidator 51f. Therefore, in the liquefier 50f according to the sixth embodiment, the configurations other than the suction unit 56d and the re-liquidator 51f are the same as those in the liquefier 50e according to the fifth embodiment, But is not necessarily referring to the same configuration.

Hereinafter, the liquefier 50f according to the sixth embodiment of the gas remelting system 1 according to the embodiment of the present invention will be described with reference to FIG.

However, since there is a difference in the configuration of the re-liquidator 51f and the suction unit 56d with respect to the liquefier 50e according to the fifth embodiment, the re-liquidator 51f, the suction unit 56d will be described in detail, but the remaining configuration is the same as that described in the liquefier 50e according to the fifth embodiment shown in Fig.

The re-liquidator 51f is provided downstream of the evaporative gas compressor 40 on the evaporative gas portion supply line L2b to heat-exchange the evaporative gas with the mixed refrigerant to liquefy it. The re-liquidator 51f may have a structure having five or more flow paths and may be, for example, a printing plate heat exchanger (PCHE).

Specifically, the re-liquidator 51f includes a gaseous mixed refrigerant and a liquid mixed refrigerant separated by a liquid mixed refrigerant oil separator 58 depressurized by the first pressure reducing valve 62b, And may have a structure in which discharged mixed refrigerant flows independently.

More specifically, the re-liquidator 51f includes an evaporation gas flow path 511f through which the evaporation gas flows, a pressure reducing valve refrigerant flow path 512f through which liquid mixed refrigerant depressurized by the first pressure reducing valve 62b flows, A suction refrigerant passage 513f through which the mixed refrigerant discharged from the oil separator 56d flows, a gas refrigerant passage 514f through which the gaseous mixed refrigerant separated by the oil separator 58 flows, and an oil separator 58 And a liquid coolant passage 515f through which the separated liquid refrigerant flows.

The mixed refrigerant flowing into the mixed refrigerant compressor (53) may be mixed with oil. At this time, the cooler 54 can cool the mixed refrigerant and transfer it to the re-liquidator 51f via the suction unit 56d so that the oil has a complete liquid phase. However, when the refrigerant mixture containing oil is heat-exchanged with the evaporation gas at a cryogenic temperature, the oil may coagulate due to the cold heat of the evaporation gas, resulting in lower heat exchange efficiency or damage to the composition.

However, the liquefied portion 50f according to the sixth embodiment of the present invention is a liquefied portion in which the mixed refrigerant in which the oil is mixed instead of the oil filter 55 (shown in Fig. 2 or Fig. 4) It is possible to prevent the solidification of the oil by configuring the heat exchanging at least part of the heat exchange.

The suction unit refrigerant passage 513f of the re-liquidator 51f is formed so as to face at least a part of the evaporation gas passage 511f in the re-liquidator 51f and then the re-liquidator 51f and the oil separator 58 The re-liquidator 51f and the oil separator 58 may be connected so that the liquid coolant passage 515f is formed so as to face at least a part of the evaporative gas passage 511f in the re-liquidator 51f .

At this time, the suction unit refrigerant passage 513f may be connected to the oil separator 58 by the mixed refrigerant circulation line L3 formed through the middle part of the re-liquidator 51f only, and the liquid refrigerant passage 515f , Which is also connected to the mixed refrigerant circulation line L3 through the intermediate portion of the re-liquidator 51f so that the intermediate portion of the re-liquidator 51f and the oil separator 58 can be connected.

The evaporated gas heat-exchanged by the mixed refrigerant in the re-liquidator 51f can be at least partially liquefied.

The suction unit 56d sucks the mixed refrigerant heat-exchanged in the re-liquidator 51f by directly receiving the mixed refrigerant compressed in the mixed refrigerant compressor 53 and compresses the mixed refrigerant compressed in the mixed refrigerant compressor 53 And supplies it to the re-liquidator 51f.

Specifically, the suction unit 56d receives the compressed mixed refrigerant from the mixed refrigerant compressor 53, sucks the liquid mixed refrigerant from the liquid refrigerant passage 515f and decompresses it, and then sucks the refrigerant from the suction unit refrigerant And can be supplied to the flow path 513f.

That is, the mixed refrigerant compressed from the mixed refrigerant compressor 53 is used as the driving fluid of the suction unit 56d, and the liquid mixed refrigerant supplied from the liquid refrigerant passage 515f is used as the suction fluid of the suction unit 56d , The driving fluid and the suction fluid may be mixed in the suction unit 56d and discharged to the re-liquidator 51f. At this time, the driving fluid may be a gas and the suction fluid may be a liquid, so that the suction unit 56d can be driven by two phases.

The suction unit 56d can have a large heat / cold section in a section relative to the pressure and enthalpy properties, thereby maximizing the cooling effect compared to a general pressure reducing valve.

Here, the suction unit 56d may be, for example, an ejector.

In the embodiment of the present invention, the first pressure reducing valve 62b can reduce the gaseous mixed refrigerant separated in the oil separator 58. [ Of course, at this time, the second pressure reducing valve 63 can reduce the pressure of the liquid mixed refrigerant separated in the oil separator 58.

In the liquefied portion 50f, the mixed refrigerant circulates in the mixed refrigerant circulation line L3 to which the components are connected.

Specifically, the mixed refrigerant flows in the order of the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the suction unit 56d, the suction unit refrigerant passage 513f of the re-liquidator 51f, and the oil separator 58 After flowing, it is separated into gas and liquid in the oil separator 58. The mixed refrigerant of the separated liquid flows into the liquid refrigerant passage 515f of the re-liquidator 51f and is sucked into the suction unit 56d. The mixed refrigerant of the separated gas flows through the gas refrigerant passage 514f And is supplied to the first pressure reducing valve 62b.

The mixed refrigerant flowing into the first pressure reducing valve 62b is supplied to the pressure reducing valve refrigerant passage 512f of the re-liquidator 51f and supplied to the receiver 52. [

As described above, in the embodiment of the present invention, the suction unit 56d, which can have a large cold / warm section in the interval of the pressure and the enthalpy property, is disposed in the liquefying unit 50f, The cooling effect is maximized by further reducing the pressure of the refrigerant.

8 is a seventh conceptional view of a liquefaction section of a gas remelting system according to an embodiment of the present invention.

8, the liquefier 50g according to the seventh embodiment includes a re-liquidator 51a, a receiver 52, a mixed refrigerant compressor 53, a cooler 54, an oil filter 55, (56e), a mixed refrigerant gas-liquid separator (57), and a mixed refrigerant circulation line (L3). The mixer 51a, the receiver 52, the mixed refrigerant compressor 53, the cooler 54, the oil filter 55, the suction unit 56e and the mixed refrigerant gas-liquid separator 57 are mixed May be connected by the refrigerant circulation line (L3), and the mixed refrigerant circulation line (L3) may circulate the mixed refrigerant.

In the liquefier 50G according to the seventh embodiment, only the configuration of the suction unit 56e in the liquefier 50a according to the first embodiment has been changed. Therefore, the configuration other than the suction unit 56e in the liquefier 50g according to the seventh embodiment can use the same reference numerals as those in the liquefier 50a according to the first embodiment, It does not refer to it.

Hereinafter, the liquefier 50g according to the seventh embodiment of the gas remelting system 1 according to the embodiment of the present invention will be described with reference to FIG.

However, as described above, since there is a difference in the configuration of only the suction unit 56e with respect to the liquefier 50a according to the first embodiment, the configuration of the suction unit 56e will be described in detail below, Is replaced with that described in the liquefier 50a according to the first embodiment shown in Fig.

The suction unit 56e sucks and discharges the mixed refrigerant heat-exchanged in the re-liquidator 51a through the mixed refrigerant compressed in the mixed refrigerant compressor 53, and varies the flow rate to be discharged in accordance with the amount of re-liquefaction of the evaporated gas .

Specifically, the suction unit 56e increases the flow rate discharged from the suction unit 56e when the amount of resuspension of the evaporation gas is greater than the predetermined resuscitation amount, and decreases the amount of resuscitation of the evaporation gas The flow rate discharged from the suction unit 56e can be reduced.

Here, the suction unit 56e may be, for example, a variable ejector.

As described above, in the embodiment of the present invention, the suction unit 56d, which can have a large cold section in the interval of the pressure and the enthalpy property, is disposed in the liquefier 50d to maximize the cooling effect .

In addition, in the embodiment of the present invention, the amount of the mixed refrigerant flowing into the re-liquidator 51a can be adjusted according to the liquefaction amount of the evaporation gas, thereby maximizing the liquefaction rate of the evaporation gas.

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

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

1: Gas re-liquefaction system 10: Liquefied gas storage tank
20: pump 30: vaporizer
40: Evaporative gas compressors 50a-g: Liquefier
51a to f: Re-liquidator 52: Receiver
53: Mixed refrigerant compressor 54: Cooler
55: Oil filter 56a to e: Suction unit
57: mixed refrigerant gas-liquid separator 58: oil separator
60: Evaporative gas liquid separator 61: Evaporated gas
62a to b: Pressure reducing valve 63: Pressure reducing valve
L1: liquefied gas supply line L2: evaporation gas supply line
L2a: Evaporative gas main supply line L2b: Evaporative gas part supply line
L3: Mixed refrigerant circulation line

Claims (8)

And a liquefied portion for liquefying the evaporated gas using a mixed refrigerant,
The liquid-
A mixed refrigerant compressor for compressing the mixed refrigerant;
A re-liquidifier for exchanging the evaporated gas with the mixed refrigerant by heat exchange;
A pressure reducing valve for decompressing the mixed refrigerant compressed in the mixed refrigerant compressor and re-introducing the mixed refrigerant into the re-liquidifier; And
And a suction unit for sucking the liquid mixed refrigerant discharged from the re-liquidator through the mixed refrigerant in the liquid phase decompressed by the pressure reducing valve, thereby further reducing the pressure of the liquid refrigerant in the depressurized liquid state. . The method according to claim 1,
The mixed refrigerant compressor is a screw type using oil for sealing and lubrication,
Further comprising an oil separator for separating the oil by gas-liquid separation of the mixed refrigerant heat-exchanged with at least a part of the evaporated gas in the re-liquidifier after being compressed in the mixed refrigerant compressor. 3. The method of claim 2,
When the pressure reducing valve is a first liquid pressure reducing valve,
The re-
An evaporation gas flow path through which the evaporation gas flows;
A reducing valve refrigerant passage through which the liquid mixed refrigerant decompressed by the first liquid pressure reducing valve flows;
A gas refrigerant passage through which the gaseous mixed refrigerant separated by the oil separator flows;
A liquid refrigerant flow path through which the liquid mixed refrigerant separated by the oil separator flows; And
And a compressed refrigerant passage through which the mixed refrigerant compressed in the mixed refrigerant compressor flows. The method of claim 3,
Wherein the compressed refrigerant flow path is formed so as to face at least a part of the evaporation gas flow path in the re-liquidator and then connected to the re-liquidator and the oil separator,
Wherein the liquid refrigerant flow path is connected to the oil separator and the re-liquidator so as to face at least a part of the evaporation gas flow path in the re-liquidifier. 5. The method of claim 4,
A cooler for cooling the mixed refrigerant compressed in the mixed refrigerant compressor;
A second liquid pressure reducing valve for reducing the liquid mixed refrigerant discharged from the oil separator;
A receiver for temporarily storing mixed refrigerant to be supplied to the mixed refrigerant compressor; And
Wherein the mixed refrigerant is circulated through the mixed refrigerant compressor, the cooler, the first liquid pressure reducing valve, the re-liquidator, the suction unit, the second liquid pressure reducing valve, the oil separator and the receiver, Wherein the gas reclamation system further comprises a line. 6. The apparatus according to claim 5,
Wherein the liquid refrigerant is supplied from the pressure reducing valve refrigerant passage to the receiver after the liquid refrigerant mixture is sucked from the liquid refrigerant passage by suction. The method according to claim 1,
The suction unit is an ejector,
Characterized in that the re-liquidator is a printing plate heat exchanger (PCHE). A vessel comprising the gas remelting system of any one of claims 1 to 7.

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