KR101957325B1 - Boil-Off Gas Reliquefaction System and Method for Vessel - Google Patents

Abstract

Disclosed is a boil-off gas (BOG) reliquefaction system for a vessel, capable of efficiently reliquefying BOG. According to the present invention, the BOG reliquefaction system for a vessel comprises: a first compressor to compress BOG; a second compressor installed in parallel to the first compressor to compress the BOG of a different flow not supplied to the first compressor; a first heat exchanger to cool the BOG compressed by the first or second compressor through heat exchange using the BOG before compressed by the first or second compressor as a refrigerant; a second heat exchanger to cool the fluid cooled by the first heat exchanger through additional heat exchange using the BOG circulated in a refrigerant cycle as the refrigerant; and first decompressor to decompress the fluid cooled by the second heat exchanger. The refrigerant cycle comprises: a second decompressor to decompress the BOG supplied to the refrigerant cycle; a third decompressor to additionally decompress the fluid decompressed by the second decompressor; fourth and fifth compressors to compress the fluid decompressed by the third compressor and used as the refrigerant in the second heat exchanger; a temperature sensor to measure the temperature of the refrigerant circulating the refrigerant cycle; and a pressure sensor to measure the pressure of the refrigerant circulating the refrigerant cycle. Moreover, the boiling point of the refrigerant in accordance with the pressure measured by the pressure sensor is calculated and thus the temperature measured by the temperature sensor is equal to or higher than the boiling point by a predetermined value (hereinafter, referred to as a third setting value).

Description

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a boil-

BACKGROUND OF THE INVENTION 1. Field of the Invention [0001] The present invention relates to a system and a method for re-liquefying a boil-off gas (BOG) generated by natural gasification of liquefied gas.

In recent years, consumption of liquefied gas such as Liquefied Natural Gas (LNG) has been rapidly increasing worldwide. The liquefied gas obtained by liquefying the gas at a low temperature has an advantage of being able to increase the storage and transport efficiency because the volume becomes very small as compared with the gas. In addition, liquefied natural gas, including liquefied natural gas, can be removed as an eco-friendly fuel with less air pollutant emissions during combustion because air pollutants can be removed or reduced during the liquefaction process.

Liquefied natural gas is a colorless transparent liquid which can be obtained by cooling methane-based natural gas to about -163 ° C and liquefying it, and has a volume of about 1/600 as compared with natural gas. Therefore, when the natural gas is liquefied and transported, it can be transported very efficiently.

However, since the liquefaction temperature of natural gas is a cryogenic temperature of -163 ° C at normal pressure, liquefied natural gas is susceptible to temperature change and is easily evaporated. As a result, the storage tank storing the liquefied natural gas is subjected to heat insulation, but the external heat is continuously transferred to the storage tank. Therefore, in the transportation of liquefied natural gas, the liquefied natural gas is naturally vaporized continuously in the storage tank, -Off Gas, BOG) occurs.

Evaporation gas is a kind of loss and is an important issue in transport efficiency. Further, when the evaporation gas accumulates in the storage tank, the internal pressure of the tank may rise excessively, and there is a risk that the tank may be damaged. Accordingly, various methods for treating the evaporative gas generated in the storage tank have been studied. Recently, a method of re-liquefying the evaporated gas and returning it to the storage tank for treating the evaporated gas, a method of returning the evaporated gas to the storage tank And a method of using it as an energy source of a consumer.

As a method for re-liquefying the evaporation gas, there is a method of re-liquefying the evaporation gas by heat exchange with the refrigerant by providing a refrigeration cycle using a separate refrigerant, a method of re-liquefying the evaporation gas itself as a refrigerant without any refrigerant .

On the other hand, there are gas-fuel engines such as DFDE, X-DF engine and ME-GI engine which can be used natural gas among the engines used in ships.

The DFDE adopts the Otto Cycle, which consists of four strokes, and injects natural gas with a relatively low pressure of about 6.5 bar into the combustion air inlet, compressing the piston as it rises.

The X-DF engine is composed of two strokes, using natural gas of about 16 bar as fuel and adopting autocycle.

The ME-GI engine consists of two strokes and employs a diesel cycle in which high pressure natural gas at around 300 bar is injected directly into the combustion chamber at the top of the piston.

A method for re-liquefying an evaporation gas by using evaporation gas itself as a refrigerant without a separate refrigerant. The evaporation gas compressed by the compressor is cooled by heat exchange with the evaporation gas before being compressed by the compressor, expanded by a JT valve, There is a method of re-liquefying a part of the gas, and a system adopting such a method is called a PRS (Partial Re-liquefaction System).

When there is a large amount of liquefied gas in the storage tank, a large amount of evaporated gas is generated, or when there is a large amount of evaporative gas to be re-liquefied , The amount of liquefaction required only by PRS may not be satisfied.

The PRS was modified to further re-liquefy the evaporation gas, and the evaporation gas could be further cooled by the refrigerant cycle using the evaporation gas itself as the refrigerant. The system employing this method was called Mane Refrigeration System).

The present invention is to provide a system and a method for liquefying a vaporization gas for marine vessels, which is configured to improve the conventional MRS, complement the problems that have been caused by operating the MRS, and to re-liquefy the evaporation gas more efficiently.

According to an aspect of the present invention, there is provided a compressor comprising: a first compressor for compressing an evaporative gas; A second compressor installed in parallel with the first compressor for compressing other flows of evaporative gas not sent to the first compressor; A first heat exchanger that cools the evaporated gas compressed by the first compressor or the second compressor by using heat as the refrigerant before the refrigerant is compressed by the first compressor or the second compressor; A second heat exchanger for further cooling the fluid cooled by the first heat exchanger by using the evaporation gas circulating the refrigerant cycle as a refrigerant for further heat exchange; And a first decompression device for decompressing the fluid cooled by the second heat exchanger, wherein the refrigerant cycle includes a second decompression device for decompressing the evaporated gas supplied to the refrigerant cycle; A third decompression device for further decompressing the fluid decompressed by the second decompression device; And a fourth compressor and a fifth compressor for compressing the fluid used as the refrigerant in the second heat exchanger after being depressurized by the third decompressor; A temperature sensor for measuring the temperature of the refrigerant circulating in the refrigerant cycle; And a pressure sensor for measuring the pressure of the refrigerant circulating in the refrigerant cycle, wherein the boiling point of the refrigerant is calculated according to the pressure measured by the pressure sensor, and the temperature measured by the temperature sensor is higher than the boiling point And a high temperature (hereinafter, a temperature higher than the boiling point is referred to as a 'third set value') is maintained.

Wherein the temperature sensor is disposed downstream of the second pressure reducing device and is capable of measuring a temperature of the fluid depressurized by the second pressure reducing device, the pressure sensor being disposed downstream of the second pressure reducing device, 2 The pressure of the fluid depressurized by the decompression device can be measured.

When the temperature measured by the temperature sensor is less than the third set value, the flow rate of the third decompression device can be reduced.

The fluid used as the refrigerant in the second heat exchanger may be branched into two flows, some of which may be supplied to the fourth compressor, and the remainder may be supplied to the fifth compressor.

The evaporated gas compressed by the fourth compressor and the evaporated gas compressed by the fifth compressor may be combined to circulate the refrigerant cycle.

The marine evaporation gas re-liquefaction system may further include one or more suction pipes installed in the refrigerant cycle for collecting droplets contained in the fluid by gravity.

Wherein the suction pipe includes a line to which the fluid decompressed by the second decompression device is sent to the third decompression device; And a line through which the fluid cooled by the second heat exchanger is sent to the second decompressor; ≪ / RTI >

The ship evaporation gas re-liquefaction system may further include a water level sensor installed in the suction pipe, and when the level of the droplet measured by the water level sensor reaches a predetermined height or more, the droplets collected in the suction pipe may be discharged.

Wherein one of the first compressor and the second compressor supplies the evaporation gas to the fuel demanding place (hereinafter, the compressor that supplies the evaporation gas to the fuel consumption place is referred to as a 'fuel supply compressor'), And the remaining compressors not supplying the evaporative gas to the fuel demanding part of the second compressor can supply the evaporative gas to the refrigerant cycle. Hereinafter, the compressor supplying the evaporative gas to the refrigerant cycle will be referred to as a 'refrigerant cycle compressor'.

Wherein the refrigerant cycle includes at least one of the refrigerant cycle compressor, the second pressure reducing device, the third pressure reducing device, the second heat exchanger, the fourth compressor or the fifth compressor, A closed loop may be formed.

The evaporated gas supplied to the refrigerant cycle may be cooled by the second heat exchanger and then sent to the second decompressor.

Wherein the refrigerant cycle includes at least one of the refrigerant cycle compressor, the second heat exchanger, the second decompressor, the third decompressor, the second heat exchanger, the fourth compressor or the fifth compressor, A closed loop connecting the 'compressor for refrigerant cycle' may be formed.

The ship evaporative gas re-liquefaction system is provided on a line that sends the evaporated gas compressed by the first compressor or the second compressor to the first heat exchanger, and is compressed by the first compressor or the second compressor And a third compressor for further compressing the evaporated gas.

The third compressor may compress the evaporation gas to 150 to 300 bar.

The third compressor may compress the evaporation gas to 150 to 170 bar.

The marine evaporation gas re-liquefaction system may further include a gas-liquid separator provided downstream of the first decompressor to separate the re-liquefied liquefied gas from the evaporated gas remaining in a gaseous state.

The evaporated gas separated by the gas-liquid separator may be combined with the evaporated gas before being used as a refrigerant in the first heat exchanger and used as a refrigerant in the first heat exchanger.

According to another aspect of the present invention, there is provided a method of operating a refrigeration cycle comprising the steps of: 1) using an evaporating gas as a refrigerant in a first heat exchanger; 2) splitting the evaporation gas used as the refrigerant of the first heat exchanger into two flows in the step 1); 3) sending the first flow to the first compressor and the remaining flow to the second compressor among the flows branched to the two flows in the step 2); 4) sending the evaporated gas compressed by the first compressor or the second compressor to the fuel consumer (hereinafter, the compressor supplying the evaporated gas to the fuel consumer is referred to as a 'fuel supply compressor'); 5) The remaining evaporation gas not used in the fuel demanding place among the evaporation gases compressed by the 'fuel supply compressor' is used as the refrigerant in the evaporation gas supplied to the first heat exchanger in the step 1) Exchanging heat by a heat exchanger; 6) sending the evaporated gas compressed by other compressors other than the 'fuel supply compressor' among the first compressor and the second compressor to the refrigerant cycle (hereinafter, the compressor supplying the refrigerant cycle evaporated gas is referred to as' Compressor '); 7) cooling the fluid cooled by the first heat exchanger in the step 5) by heat exchange using the evaporator gas circulating in the refrigerant cycle as the refrigerant by the second heat exchanger; And 8) depressurizing the fluid cooled by the second heat exchanger in step 7), and the evaporation gas circulating in the refrigerant cycle is compressed by the compressor for the refrigerant cycle ; 5-2) cooling by the second heat exchanger after being compressed in step 5-1); 5-3) After cooling in step 5-2), the pressure is reduced by the second pressure reducing device; 5-4) depressurizing in the step 5-3), and further depressurizing by the third decompressor; 5-5) using the refrigerant as a refrigerant in the second heat exchanger after further reducing the pressure in step 5-4); And 5-6) using the refrigerant as the refrigerant in the second heat exchanger in the step 5-5), then branching into two flows; 5-7) one of the two flows branched in the step 5-6) is sent to the fourth compressor and the remaining flow is sent to the fifth compressor; And 5-8) combining the evaporated gas compressed by the fourth compressor and the evaporated gas compressed by the fifth compressor, wherein the boiling point of the refrigerant circulating in the refrigerant cycle And the temperature of the refrigerant circulating in the refrigerant cycle is maintained at a temperature higher than the boiling point by a predetermined value (hereinafter, a temperature higher than the boiling point is referred to as a third set value) A gas re-liquefaction method is provided.

When the temperature of the refrigerant circulating in the refrigerant cycle is less than the third set value, the flow rate of the third pressure reducing device can be reduced.

The droplets contained in the refrigerant circulating in the refrigerant cycle can be collected at the lower portion of the suction pipe by gravity.

According to the present invention, the evaporation gas supplied to the refrigerant cycle (RC) is further depressurized by the third decompression device (425) as well as the second decompression device (420) to be used as the refrigerant of the second heat exchanger Therefore, the re-liquefaction efficiency and the amount of re-liquefaction can be further increased.

According to an embodiment of the present invention, a boiling point according to the pressure of the refrigerant measured by the pressure sensor 615 is calculated, and the temperature of the refrigerant measured by the temperature sensor 610 is measured by the pressure sensor 615 So that the temperature of the refrigerant circulating in the refrigerant cycle RC can be maintained within a range in which no droplet is generated.

According to the embodiment of the present invention, since the suction pipe 620 is provided to collect the droplets in the suction pipe 620, it is possible to prevent the droplets from being introduced into the second decompressor 420 or the third decompressor 425 have.

According to an embodiment of the present invention, when the level of the liquid droplets collected in the suction pipe 620 is too high, the flow of the fluid flowing into the second decompressor 420 or the third decompressor 425 is cut off, It is possible to more thoroughly prevent the droplet from being introduced into the third decompression device 420 or the third decompression device 425.

1 is a schematic view of a vaporization gas re-liquefaction system for a ship according to a first preferred embodiment of the present invention.
2 is a schematic view of a vaporization gas re-liquefaction system for ships according to a second preferred embodiment of the present invention.
FIG. 3 is a schematic view of a vaporization gas re-liquefaction system for a ship according to a third preferred embodiment of the present invention.
4 is a graph schematically illustrating the phase change of methane with temperature and pressure.
5 is a graph showing the temperature values of methane according to the heat flow rate under different pressures, respectively.
6 and 7 are graphs showing the amount of liquefaction according to the evaporation gas pressure in a PRS (Partial Re-liquefaction System).

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the accompanying drawings. The system and method for liquefying the ship's evaporative gas according to the present invention can be applied to various applications such as a ship equipped with an engine using natural gas as fuel, a ship including a liquefied gas storage tank, or an offshore structure. In addition, the following examples can be modified in various forms, and the scope of the present invention is not limited to the following examples.

The fluid in each line of the present invention may be in any one of a liquid state, a gas-liquid mixed state, a gas state, and a supercritical fluid state, depending on operating conditions of the system.

1 is a schematic view of a vaporization gas re-liquefaction system for a ship according to a first preferred embodiment of the present invention.

Referring to FIG. 1, the evaporative gas re-liquefaction system for a ship according to the present embodiment includes a first heat exchanger 110, a first compressor 210, a second compressor 220, a second heat exchanger 120, Device 410, and a refrigerant cycle (RC).

The first heat exchanger 110 is operated by the first compressor 210 or the second compressor 220 by using the evaporation gas before being compressed by the first compressor 210 or the second compressor 220 as a refrigerant. Cool the compressed evaporated gas.

The evaporating gas used as the refrigerant in the first heat exchanger 110 may be evaporated gas discharged from the storage tank T. [

The evaporated gas used as the refrigerant in the first heat exchanger 110 is diverted into two flows, one stream is sent to the first compressor 210 and the other stream is sent to the second compressor 220.

The first compressor 210 is used as a refrigerant in the first heat exchanger 110, and then compresses one of the evaporative gases branched into two flows. The first compressor 210 may be a multi-stage compressor, and a first cooler 310 may be installed downstream of the first compressor 210 to cool the evaporated gas compressed by the first compressor 210.

The second compressor 220 is installed in parallel with the first compressor 210 and is used as a refrigerant in the first heat exchanger 110 and then sent to the first compressor 210 among the evaporated gases branched into two flows Compress the remaining flow. The second compressor 220 may be a multi-stage compressor, and a second cooler 320 may be installed downstream of the second compressor 220 to cool the evaporated gas compressed by the second compressor 220.

Either one of the first compressor 210 and the second compressor 220 supplies the evaporative gas to the fuel consumer E and the other one supplies the evaporative gas to the refrigerant cycle RC. In addition, among the evaporated gas compressed by the compressor that supplies the evaporated gas to the fuel demand site E, the surplus evaporated gas not used in the fuel demand site E is sent to the first heat exchanger 110 and subjected to a liquefaction process .

The fuel demand (E) includes the ME-GI engine, which uses approximately 300 bar of natural gas as fuel, the X-DF engine, which uses approximately 16 bar of natural gas as fuel, and DF An engine (DFGE, DFDE), and a gas combustion unit (GCU).

The compressor that supplies the fuel to the fuel demand destination E among the first compressor 210 and the second compressor 220 when the fuel demanding entity E is an engine compresses the evaporation gas at the required pressure of the fuel demand site E .

The ship's regulations require that a compressor that supplies fuel to the engine be designed with redundancy in case of an emergency. Redundancy design means that when one of the compressors can not be used for reasons of failure, maintenance, etc., It means to design to be able to use.

In the present embodiment, the first compressor 210 and the second compressor 220 may serve as redundancies. Conventionally, one of the first compressor 210 and the second compressor 220 evaporates (E), and the other unused one is put in the standby state. If the compressor which supplied the evaporative gas to the fuel demand point (E) can not be used, ) State compressor to supply the evaporative gas to the fuel consumer (E).

However, according to the conventional operating method, although the probability that the compressor used as the evaporative gas can not be used at the fuel demand site E is low and the duration is not long even if it occurs, the emergency situation There is a problem in that a redundant compressor is installed and the extra compressor is kept in a stand-by state in order to prepare, so that the actual dangerous cost is wasted.

According to the present embodiment, when both the first compressor 210 and the second compressor 220 can be normally used, one is used for supplying the fuel to the fuel consumer E and the other is used for the refrigerant cycle When the compressor used for supplying the evaporative gas to the fuel demand site E can not be used, the evaporative gas is supplied to the refrigerant cycle RC to regain the re-liquefaction amount and the re-liquefaction efficiency And supplies the evaporated gas to the fuel consuming destination E by means of the compressor that supplied the evaporative gas to the refrigerant cycle RC.

Therefore, according to the present embodiment, there is an advantage that the re-liquefaction amount and the re-liquefaction efficiency can be improved by utilizing an extra compressor installed to prepare for an emergency situation while satisfying the ship regulations requiring redundancy design.

It is preferable that the first compressor 210 and the second compressor 220 are compressors having the same performance so that they can serve as redundancies.

The second heat exchanger 120 compresses the refrigerant by the first compressor 210 or the second compressor 220 using the evaporation gas circulating the refrigerant cycle RC as the refrigerant, Is further cooled by heat exchange. The fluid further cooled by the second heat exchanger (120) is sent to the first pressure reducing device (410).

According to the present embodiment, the evaporated gas is further cooled not only in the first heat exchanger 110 but also in the second heat exchanger 120 so that the evaporated gas cooled only by the first heat exchanger 110 flows into the first decompressor 410, the evaporated gas in a lowered temperature state is sent to the first pressure reducing device 410, so that the re-liquefaction efficiency and the liquefaction amount are increased. The following is a detailed description.

4 is a graph schematically illustrating the phase change of methane with temperature and pressure. Referring to FIG. 4, methane enters a supercritical fluid state at a temperature of approximately -80 占 폚 or higher and a pressure of approximately 55 bar or higher. That is, in the case of methane, the critical point is about -80 ° C, 55 bar. The supercritical fluid state is a third state different from the liquid state or gas state.

When the evaporation gas has a temperature lower than the critical point at a pressure equal to or higher than the critical point, it may be in a state similar to the supercritical fluid state having a higher density than the general liquid state. The evaporation gas having a pressure higher than the critical point and a temperature lower than the critical point State is hereinafter referred to as "high-pressure liquid state ".

The evaporation gas sent to the first heat exchanger 110 for the re-liquefaction process may be in a gaseous state or in a supercritical fluid state depending on the degree of compression. When the evaporated gas sent to the first heat exchanger 110 is in a gaseous state, the evaporated gas in the gaseous state passes through the first heat exchanger 110 and the temperature is lowered to become a mixed state of the liquid and the gas, 1 heat exchanger 110 is in the supercritical fluid state, the fluid in the supercritical fluid state passes through the first heat exchanger 110 and becomes low in temperature to be in the " high pressure liquid state ".

The temperature of the fluid cooled by the first heat exchanger 110 is lowered while passing through the second heat exchanger 120. When the fluid that has passed through the first heat exchanger 110 is in a mixed state of liquid and gas , The fluid in the liquid mixed state with the gas passes through the second heat exchanger 120 and becomes lower in temperature so that the ratio of the liquid becomes higher or becomes the liquid state and passes through the first heat exchanger 110 When the fluid is in the " high pressure liquid state ", the fluid in the "high pressure liquid state" passes through the second heat exchanger 120 and becomes the "high pressure liquid state "

In addition, even if the fluid that has passed through the second heat exchanger 120 is in the "high pressure liquid state ", the fluid of the" high pressure liquid state "through the second heat exchanger 120 passes through the first pressure reducing device 410 The pressure is lowered to become a liquid state or a mixture state of liquid and gas.

Even if the evaporation gas is lowered to the same degree (P in FIG. 4) by the first decompression device 410, the temperature is lower than that in the case where the temperature is lowered in a higher state (X → X ' (Y - > Y 'in Fig. 4), the ratio of liquid becomes higher. Further, if the temperature can be further lowered, the evaporation gas can theoretically be 100% re-liquefied (Z → Z 'in FIG. 4). Therefore, when the fluid cooled by the first heat exchanger 110 is further cooled by the second heat exchanger 120 and then sent to the first pressure reducing device 410, the re-liquefaction efficiency and the liquefaction amount are increased.

The first decompression device 410 compresses the evaporated gas cooled by the first heat exchanger 110 and the second heat exchanger 120 after being compressed by the first compressor 210 or the second compressor 220, . The first decompression device 410 includes all the means capable of decompressing and cooling the evaporation gas, and may be an expansion valve such as a Joule-Thomson valve or an expander. In the present embodiment, it is preferable that the first pressure reducing device 410 is an expansion valve. The expansion valve has the advantage that the price is lower than the inflator and the risk of failure is less.

The compression process by the first compressor 210 or the second compressor 220 and the cooling process by the first heat exchanger 110 and the second heat exchanger 120 are performed by the first decompressor 410 or the second decompressor 410, Some or all of the evaporated gas that has undergone the process is re-liquefied.

The marine evaporation gas re-liquefaction system of this embodiment may further include a gas-liquid separator 500 disposed downstream of the first decompressor 410 for separating the re-liquefied liquefied gas from the remaining vaporized gas .

The liquefied gas separated by the gas-liquid separator 500 can be sent to the storage tank T and the evaporated gas separated by the gas-liquid separator 500 can be sent to the evaporator 200 before being used as a refrigerant in the first heat exchanger 110 And can be used as a refrigerant in the first heat exchanger 110. [

When the first heat exchanger 110 uses the evaporated gas discharged from the storage tank T as a refrigerant, the evaporated gas separated by the gas-liquid separator 500 is mixed with the evaporated gas discharged from the storage tank T And may be sent to the first heat exchanger 110.

The evaporated gas separated by the gas-liquid separator 500 may be separately used as a refrigerant in the first heat exchanger 110 without being merged with the evaporated gas before being used as a refrigerant in the first heat exchanger 110 In this case, the first heat exchanger 110 may be composed of three flow paths.

If the ship evaporative gas re-liquefaction system of this embodiment does not include the gas-liquid separator 500, the evaporated gas partially or fully re-liquefied may be sent directly to the storage tank T from the first decompressor 410.

The refrigerant cycle RC in which the evaporation gas used as the refrigerant in the second heat exchanger 120 is circulated includes the second decompression device 420, the third decompression device 425, the fourth compressor 240, A compressor 245 is included.

The evaporated gas compressed by the first compressor 210 or the second compressor 220 and then supplied to the refrigerant cycle RC is cooled by the second heat exchanger 120 and then sent to the second decompressor 420 Loses.

The second decompression device 420 reduces the temperature by reducing the pressure of the evaporation gas supplied to the refrigerant cycle RC after being compressed by the first compressor 210 or the second compressor 220. The second decompression device 420 includes all the means capable of decompressing and cooling the evaporation gas, and may be an expansion valve such as a Joule-Thomson valve or an expander. In the present embodiment, it is preferable that the second decompressor 420 is an expander.

The third pressure reducing device 425 further depressurizes the fluid depressurized by the second pressure reducing device 420 to further lower the temperature. The third pressure reducing device 425 includes all means capable of cooling down the evaporation gas by cooling it, and may be an expansion valve such as a Joule-Thomson valve or an expansion valve. In the present embodiment, it is preferable that the third pressure reducing device 425 is an inflator.

The fluid sequentially depressurized by the second pressure reducing device 420 and the third pressure reducing device 425 is supplied to the second heat exchanger 120 so that the fluid cooled by the first heat exchanger 110 is further supplied It is used as refrigerant for cooling.

The evaporated gas supplied to the refrigerant cycle (RC) after being compressed by the first compressor (210) or the second compressor (220) is supplied to the second heat exchanger (120) before being depressurized by the second decompressor It can pass. In this case, the evaporated gas supplied to the refrigerant cycle (RC) after being compressed by the first compressor (210) or the second compressor (220) is heat-exchanged by the second heat exchanger (120) 2 decompressed by the second decompression device 420, cooled secondarily, decompressed by the third decompression device 425 to be thirdly cooled, and then sent again to the second heat exchanger 120 to be used as a refrigerant.

The fourth compressor 240 and the fifth compressor 245 compress the fluid used as the refrigerant in the second heat exchanger 120 to keep the pressure average of the evaporated gas circulating in the refrigerant cycle RC constant It plays a role.

The fourth compressor 240 and the fifth compressor 245 are connected in parallel, while the second decompressor 420 and the third decompressor 425 are connected in series to depressurize the fluid in sequence, The fluid used as the refrigerant in the heat exchanger 120 is diverted into two flows, one stream is sent to the fourth compressor 240 and the remaining stream is sent to the fifth compressor 245. The evaporated gas compressed by the fourth compressor 240 and the evaporated gas compressed by the fifth compressor 245 are combined to circulate the refrigerant cycle RC.

The fourth compressor 240 may be driven by the power generated by the second decompressor 420 forming the first compressor 420 and the second compressor 420 expanding the fluid, The third decompressor 425 and the second compressor 42 can be driven by the power generated by the third decompressor 425 while expanding the fluid.

A fourth cooler 340 for cooling the evaporated gas compressed by the fourth compressor 240 or the fifth compressor 245 may be installed downstream of the fourth compressor 240 and the fifth compressor 245 have. In the case where the present invention includes the fourth cooler 340, the evaporated gas compressed by the fourth compressor 240 and the evaporated gas compressed by the fifth compressor 245 are combined and then supplied to the fourth cooler 340 .

In the evaporative gas re-liquefaction system for a ship according to the present embodiment, the flow in which the evaporated gas compressed by the fourth compressor 240 and the evaporated gas compressed by the fifth compressor 245 are combined is supplied to the upstream side of the first compressor 210 The first compressor 210 may be connected to the second compressor 220 and the first compressor 210 may be connected to the second compressor 220. The second compressor 220 may be connected to the second compressor 220, Respectively.

When the evaporated gas compressed by the first compressor 210 is supplied to the fuel consumer E and the evaporated gas compressed by the second compressor 220 is supplied to the refrigerant cycle RC, The first compressor 220, the second decompressor 420, the third decompressor 425, the second heat exchanger 120, the fourth compressor 240 or the fifth compressor 245 and the second compressor 220 A refrigerant cycle RC of the closed loop to be connected is formed. When the evaporated gas supplied to the refrigerant cycle RC is cooled by the second heat exchanger 120 and then sent to the second decompressor 420, the second compressor 220, the second heat exchanger 120, The second pressure reducing device 420, the third pressure reducing device 425, the second heat exchanger 120, the fourth compressor 240 or the fifth compressor 245 and the second compressor 220 are connected to each other A refrigerant cycle RC of a closed loop is formed.

When the evaporated gas compressed by the first compressor 210 is supplied to the refrigerant cycle RC and the evaporated gas compressed by the second compressor 220 is supplied to the fuel consumer E, The first compressor 210, the second decompressor 420, the third decompressor 425, the second heat exchanger 120, the fourth compressor 240 or the fifth compressor 245, A refrigerant cycle RC of the closed loop to be connected is formed. When the evaporated gas supplied to the refrigerant cycle RC is cooled by the second heat exchanger 120 and then sent to the second decompressor 420, the first compressor 210, the second heat exchanger 120, The second pressure reducing device 420, the third pressure reducing device 425, the second heat exchanger 120, the fourth compressor 240 or the fifth compressor 245, and the first compressor 210 again A refrigerant cycle RC of a closed loop is formed.

According to the present invention, any one of the first compressor (210) and the second compressor (220) can be selected to supply evaporative gas to the fuel consumer (E) or the first heat exchanger (110) And the refrigerant cycle (RC) can be circulated to the first heat exchanger (110) with the evaporated gas compressed by the other compressor that does not supply the evaporated gas, so that the operation of the system is advantageous.

In addition, according to the present invention, there is an advantage that the re-liquefaction efficiency and re-liquefaction amount of the evaporation gas can be increased by utilizing the redundancy compressor which is conventionally installed on the ship but is not normally used.

In addition, according to the present invention, the evaporation gas supplied to the refrigerant cycle (RC) is further depressurized by the third decompression device (425) as well as the second decompression device (420) Since it is used as a refrigerant, the re-liquefaction efficiency and the amount of re-liquefaction can be further increased.

According to this embodiment, nitrogen may be injected into the refrigerant cycle RC so that the fluid in which the evaporation gas and nitrogen are mixed circulates in the refrigerant cycle RC and is used as the refrigerant in the second heat exchanger 120.

The evaporative gas re-liquefaction system for a ship according to the present embodiment is installed on a line for sending the evaporated gas compressed by the first compressor 210 or the second compressor 220 to the first heat exchanger 110, 210) or a third compressor (230) for further compressing the evaporated gas compressed by the second compressor (220). A third cooler 330 for cooling the evaporated gas compressed by the third compressor 230 may be installed downstream of the third compressor 230.

The reason why the third compressor 230 further compresses the evaporated gas that is compressed by the first compressor 210 or the second compressor 220 and then sent to the first heat exchanger 110 is that the re- The pressure of the evaporation gas is increased to increase the liquefaction amount and the re-liquefaction efficiency.

FIG. 5 is a graph showing the temperature values of methane according to the heat flow rate under different pressures. Referring to FIG. 5, it can be seen that the higher the pressure of the evaporation gas subjected to the re-liquefaction process, the higher the efficiency of the self-heat exchange. Self-heat self-exchange means that cold evaporation gas itself is used as refrigerant and heat is exchanged at high temperature evaporation gas.

5 (a) shows the state of each fluid in the upstream and downstream of the second heat exchanger 120 when the ship's evaporative-gas re-liquefaction system of the present embodiment does not include the third compressor 230 And FIG. 5 (b) shows the state of each fluid at the upstream and downstream sides of the second heat exchanger 120 when the ship's evaporative gas re-liquefaction system of the present embodiment includes the third compressor 230.

5, the evaporated gas supplied to the refrigerant cycle (RC) after being compressed by the first compressor (210) or the second compressor (220) is cooled by the second heat exchanger (120) 420 and then supplied to the second heat exchanger 120 again.

The uppermost graph I of FIGS. 5A and 5B shows the fluid state at the point P1 in FIG. 1 supplied to the second heat exchanger 120, and the lowermost graph L shows the second heat exchange 1, which is fed back to the second heat exchanger 120 to be used as a refrigerant after passing through the first and second decompression devices 120 and 420, The overlapped graph J shows the fluid state at the point P3 in FIG. 1, which is supplied to the second heat exchanger 120 after passing through the first heat exchanger 110. In FIG.

Since the fluid used as the refrigerant is deprived of the cold heat during the heat exchange process and the temperature gradually increases, the graph L advances from the left to the right according to the passage of time, and the fluid cooled by heat exchange with the refrigerant is cooled from the refrigerant in the heat exchange process Since the temperature is gradually decreased due to the supply, the graph I and the graph J proceed from right to left as time passes.

A graph K in the middle part of FIGS. 5 (a) and 5 (b) is a combination of graph I and graph J. That is, the fluid used as the refrigerant in the second heat exchanger 120 is drawn in a graph L, and the fluid cooled by heat exchange with the refrigerant in the second heat exchanger 120 is drawn in a graph K.

In designing the heat exchanger, the temperature and the heat flow of the fluid supplied to the heat exchanger (that is, the fluid at the points P1, P2, and P3 in FIG. 1) are fixed and the temperature of the fluid used as the refrigerant is controlled So that the logarithmic mean temperature difference (LMTD) can be minimized while preventing the graph L from crossing over the graph K so that the graph L does not appear above the graph K.

The logarithmic mean temperature difference (LMTD) is the temperature difference between the low-temperature fluid and the low-temperature fluid in the opposite direction and the opposite direction. In the case of countercurrent flow, the low-temperature fluid passes through the heat exchanger And the temperature after the high-temperature fluid has passed through the heat exchanger is th2 and d1 = th2-tc1, d2 = th1-tc2, d1) / ln (d2 / d1). As the logarithmic mean temperature difference is smaller, the efficiency of the heat exchanger increases.

The logarithmic mean temperature difference (LMTD) on the graph is represented by the interval between the low temperature fluid used as the coolant (graph L in FIG. 5) and the high temperature fluid cooled by heat exchange with the coolant (graph K in FIG. 5) (B) of FIG. 5 shows that the interval between the graph L and the graph K is narrower than the interval between the graph L and the graph K.

This difference is due to the fact that the initial value of the graph J, which is the point indicated by the round circle, that is, the pressure of the fluid at the point P3 in FIG. 1 fed to the second heat exchanger 120 after passing through the first heat exchanger 110 (B) of Fig. 5 is higher than that of Fig. 5 (a).

That is, as a result of the simulation, in the case of FIG. 5 (a) without the third compressor 230, the fluid at the point P3 in FIG. 1 may be approximately -111 ° C., , The fluid at point P3 in FIG. 1 may be approximately -90 DEG C, 50 bar. Under these initial conditions, the heat exchanger may be used to minimize the logarithmic mean temperature difference (LMTD) In the case of FIG. 5 (b) in which the pressure of the evaporative gas passing through the re-liquefaction process is high, the efficiency of the heat exchanger becomes higher, and as a result, the total liquefaction amount and re-liquefaction efficiency of the entire system become high.

5A, when the flow rate of the evaporation gas used as the refrigerant in the second heat exchanger 120 is approximately 6401 kg / h, the refrigerant is heat-exchanged with the refrigerant from the fluid (graph L) used as the refrigerant, (Graph K) is approximately 585.4 kW and the flow rate of the re-liquefied vapor is approximately 3441 kg / h.

5B, when the flow rate of the evaporative gas used as the refrigerant in the second heat exchanger 120 is approximately 5368 kg / h, the refrigerant is heat-exchanged with the refrigerant from the fluid (graph L) (Graph K) is approximately 545.2 kW, and the flow rate of the re-liquefied evaporation gas is approximately 4325 kg / h.

That is, if the pressure of the evaporative gas including the third compressor 230 is re-liquefied, a larger amount of the evaporated gas can be re-liquefied even if less refrigerant is used.

When the evaporator is further cooled by the third compressor 230 to increase the amount of re-liquefaction and re-liquefaction efficiency, the entire amount of evaporation gas can be re-liquefied without further cooling the evaporator by the second heat exchanger 120 The time required to supply the evaporative gas to the refrigerant cycle RC is reduced and thus the effect of the redundancy design that the compressor for supplying the evaporative gas to the fuel demand site E is prepared is sufficiently secured can do.

In the meantime, it will be appreciated that the evaporative gas re-liquefaction system of the present embodiment may advantageously include the third compressor 230 in some cases, and the preferred pressure for the third compressor 230 to compress the evaporative gas will be as follows.

6 and 7 are graphs showing the amount of liquefaction according to the evaporation gas pressure in a PRS (Partial Re-liquefaction System). The evaporative gas to be re-liquefied refers to the evaporated gas which is cooled and re-liquefied, and is named to distinguish it from the evaporative gas used as the refrigerant.

6 and 7 are graphs showing the re-liquefaction amount according to the evaporation gas pressure in the PRS, so that the re-liquefaction amount is lower than that of the MRS in which the evaporation gas is additionally re-liquefied by the evaporation gas circulating in the refrigerant cycle . In the case of MRS, about 3300 kg of evaporative gas per hour can be re-liquefied.

6 and 7, it can be seen that when the pressure of the evaporation gas is in the vicinity of 150 to 170 bar, the re-liquefaction amount shows the maximum value, and when the pressure is 150 to 300 bar, there is almost no change in the liquefaction amount.

The evaporated gas compressed by the first compressor 210 and the second compressor 220 at the required pressure of the fuel consumer E is sent to the fuel consumer E and the evaporated gas is fed to the fuel consumer E A surplus evaporated gas not used in the fuel demand point E is sent to the first heat exchanger 110 among the evaporated gases compressed by the supplying compressor to be subjected to a liquefaction process so that the evaporation gas re- When the third compressor (230) is not included, a part of the evaporated gas compressed at the required pressure of the fuel consuming area (E) is sent to the first heat exchanger (110)

In the case of an engine using natural gas of 150 bar or more, such as ME-GI engine in which the demand for fuel (E) is natural gas of about 300 bar, the pressure required by the fuel demand point (E) However, when the fuel demand (E) is consumed at about 16 bar of the natural gas as the fuel, the X- In the case of a DF engine or a DF engine (DFGE, DFDE) using natural gas of about 6.5 bar as a fuel, in the case of an engine using natural gas less than 150 bar as fuel, the third compressor 230, And then subjected to a re-liquefaction process.

Further, it is preferable that the third compressor 230 compress the evaporation gas to approximately 150 to 300 bar, more preferably approximately 150 to 170 bar, so as to secure the maximum amount of resolidification . Further, since the energy consumed by the third compressor 230 can be reduced as the degree to which the third compressor 230 compresses the evaporation gas is reduced, the third compressor 230 further preferably has a capacity of about 150 bar So that the evaporation gas can be compressed.

It is generally sufficient that the third compressor 230 has approximately one half capacity of the first compressor 210 or the second compressor 220. [

On the other hand, when the amount of the liquefied gas stored in the storage tank T is small and the amount of the evaporated gas discharged from the storage tank T is small, or when there is a large amount of evaporated gas used as fuel in the fuel demand site E such as the engine The second heat exchanger 120 bypasses the first heat exchanger 120 and the second heat exchanger 120 directly bypasses the first heat exchanger 110. In this case, It may be sent to the decompression apparatus 410 and operated in the same manner as PRS.

Since it is not necessary to supply the refrigerant to the second heat exchanger 120 when the evaporative gas passing through the re-liquefaction process is cooled only by the first heat exchanger 110 and the second heat exchanger 120 is bypassed, It may not supply the evaporation gas to the cycle RC.

2 is a schematic view of a vaporization gas re-liquefaction system for ships according to a second preferred embodiment of the present invention.

2, the boil-off gas re-liquefaction system for a ship according to the second embodiment further includes a temperature sensor 610 and a pressure sensor 615 as compared with the boil-off gas re-liquefaction system of the first embodiment shown in Fig. 1 There are differences in the points, and the differences are mainly described below. The detailed description of the same components as those of the evaporation gas re-liquefaction system for marine vessels of the first embodiment described above will be omitted.

Referring to FIG. 2, the evaporating gas re-liquefaction system for a ship according to the present embodiment includes a first heat exchanger 110, a first compressor 210, a second compressor 220, a second heat exchanger A first pressure reducing device 120, a first pressure reducing device 410, and a refrigerant cycle RC.

The refrigerant cycle RC of the present embodiment includes a second decompression device 420, a third decompression device 425, a fourth compressor 240, and a fifth compressor 245 as in the first embodiment .

The vessel evaporation gas re-liquefaction system according to the present embodiment may further include at least one of the third compressor 230 and the gas-liquid separator 500 as in the first embodiment, The evaporated gas compressed by the first compressor 210 or the second compressor 220 is cooled only by the first heat exchanger 110 and the second heat exchanger 120 is bypassed, And may be sent to the decompression apparatus 410.

In addition, the second decompressor 420 and the third decompressor 425 of the present embodiment are expanders including a plurality of blades.

The refrigerant cycle RC of this embodiment may further include at least one suction pipe 620, unlike the first embodiment.

 When the fluid containing the droplet is sent to the third pressure reducing device 425, a blade rotating at a high speed may be used as the pressure reducing device, There is a possibility that a liquid droplet may enter the nozzle and damage the blade.

Therefore, in this embodiment, the suction pipe 620 is provided in a line to which the fluid decompressed by the second decompression device 420 is sent to the third decompression device 425, so that the droplet enters the third decompression device 425 . The fluid passes through the suction pipe 620 and the liquid contained in the fluid is collected under the suction pipe 620 by gravity and the gas component rises to the upper portion of the suction pipe 620.

2, the suction pipe 620 is installed between the second decompression device 420 and the third decompression device 425, but the evaporation gas supplied to the refrigerant cycle RC is supplied to the second heat exchanger 120 The fluid cooled by the second heat exchanger 120 can be contained in the fluid cooled by the second heat exchanger 120. Therefore, The suction pipe 620 may be installed in a line to be sent to the decompression device 420. Of course, the line to which the fluid depressurized by the second pressure reducing device 420 is sent to the third pressure reducing device 425 and the line that the fluid cooled by the second heat exchanger 120 is sent to the second pressure reducing device 420 The suction pipe 620 may be installed on the line.

The liquid level sensor 630 may be installed in the suction pipe 620 and the droplets collected in the suction pipe 620 may be discharged when the level of the liquid level measured by the level sensor 630 becomes equal to or higher than a certain height.

The refrigerant cycle RC of the present embodiment includes a temperature sensor 610 and a pressure sensor 615, unlike the first embodiment. The temperature sensor 610 measures the temperature of the refrigerant circulating in the refrigerant cycle RC and the pressure sensor 615 measures the pressure of the refrigerant circulating in the refrigerant cycle RC.

According to the present embodiment, the boiling point (i.e., the temperature at which the droplet is generated) according to the pressure of the refrigerant measured by the pressure sensor 615 is calculated and the temperature of the refrigerant measured by the temperature sensor 610 is detected by the pressure sensor 615 So that it does not fall below the boiling point according to the pressure measured by the pressure sensor. That is, the temperature of the refrigerant circulating in the refrigerant cycle RC is maintained in a range in which no droplet is generated.

Specifically, the temperature measured by the temperature sensor 610 is set to a temperature higher than the boiling point according to the pressure measured by the pressure sensor 615 (hereinafter referred to as a "third set value" ) Or more.

On the other hand, the refrigerant circulating in the refrigerant cycle (RC) is cooled by the second heat exchanger (120) and the fluid cooled by the second decompressor (420) after being cooled by the second heat exchanger The fluid that has been decompressed by the second decompression device 420 and then decompressed by the third decompression device 425 is the lowest temperature.

That is, the probability that the fluid decompressed by the second decompressor 420 and the fluid decompressed by the third decompressor 425 are high, and the fluid decompressed by the third decompressor 425 is the second When the droplet is generated in the fluid depressurized by the second pressure reducing device 420, the droplet is introduced into the third pressure reducing device 425, The pressure reducing device 425 may be damaged.

The temperature sensor 610 and the pressure sensor 615 are installed downstream of the second decompressor 420 and are cooled by the second heat exchanger 120 and then decompressed by the second decompressor 420 It is desirable to measure the pressure and temperature of the fluid.

It is preferable that the suction pipe 620 is also installed between the second decompressor 420 and the third decompressor 425 and more preferably the suction pipe 620 is provided between the temperature sensor 610 and the pressure sensor 615 And downstream of the third pressure reducing device 425. [

According to this embodiment, in order to maintain the temperature measured by the temperature sensor 610 at the third set value or more, when the temperature measured by the temperature sensor 610 becomes less than the third set value, 425 can be reduced.

When the flow rate of the third decompression device 425 is reduced, the flow rate of the refrigerant circulating in the refrigerant cycle RC is reduced, so that the average temperature of the refrigerant circulating in the refrigerant cycle RC becomes higher and the probability of occurrence of the droplet becomes lower.

FIG. 3 is a schematic view of a vaporization gas re-liquefaction system for a ship according to a third preferred embodiment of the present invention.

3, the boil-off gas re-liquefaction system for a ship according to the third embodiment further includes a suction pipe 620 and a bypass line BL in comparison with the boil-off gas re-liquefaction system for a ship according to the first embodiment shown in Fig. 1 There are differences in the following, and the differences are mainly described below. The detailed description of the same components as those of the evaporation gas re-liquefaction system for marine vessels of the first embodiment described above will be omitted.

Referring to FIG. 3, the evaporative gas re-liquefaction system for a ship according to the present embodiment includes a first heat exchanger 110, a first compressor 210, a second compressor 220, a second heat exchanger A first pressure reducing device 120, a first pressure reducing device 410, and a refrigerant cycle RC.

The refrigerant cycle RC of the present embodiment includes a second decompression device 420, a third decompression device 425, a fourth compressor 240, and a fifth compressor 245 as in the first embodiment .

The vessel evaporation gas re-liquefaction system according to the present embodiment may further include at least one of the third compressor 230 and the gas-liquid separator 500 as in the first embodiment, The evaporated gas compressed by the first compressor 210 or the second compressor 220 is cooled only by the first heat exchanger 110 and the second heat exchanger 120 is bypassed, And may be sent to the decompression apparatus 410.

In addition, the second decompressor 420 and the third decompressor 425 of the present embodiment are expanders including a plurality of blades.

Unlike the first embodiment, the refrigerant cycle (RC) of the present embodiment further includes one or more suction pipes 620.

 When the fluid containing the droplet is sent to the third pressure reducing device 425, a blade rotating at a high speed may be used as the pressure reducing device, There is a possibility that a liquid droplet may enter the nozzle and damage the blade.

Therefore, in the present embodiment, the suction pipe 620 is provided in the line for sending the fluid decompressed by the second decompressor 420 to the third decompressor 425, so that the droplet does not flow into the third decompressor 425 . The fluid passes through the suction pipe 620 and the liquid contained in the fluid is collected under the suction pipe 620 by gravity and the gas component rises to the upper portion of the suction pipe 620.

3 shows that the suction pipe 620 is installed between the second decompression device 420 and the third decompression device 425 but the evaporation gas supplied to the refrigerant cycle RC is supplied to the second heat exchanger 120 The fluid cooled by the second heat exchanger 120 can be contained in the fluid cooled by the second heat exchanger 120 and the fluid cooled by the second heat exchanger 120 can be supplied to the second heat exchanger 120. [ The suction pipe 620 may be installed in a line to the decompression device 420. Of course, the line for sending the fluid decompressed by the second decompression device 420 to the third decompressor 425 and the line for sending the fluid cooled by the second heat exchanger 420 to the second decompressor 420 The suction pipe 620 may be provided on both sides.

The suction pipe 620 is provided with a water level sensor 630. When the water level measured by the water level sensor 630 is equal to or higher than the first predetermined value, the droplets collected in the suction pipe 620 can be discharged. If the level of the liquid drops measured by the water level sensor 630 is equal to or greater than the first predetermined value, an alarm may be generated so as to inform the time when the liquid droplets collected in the suction pipe 620 are discharged.

The refrigerant cycle RC of the present embodiment is different from the first embodiment in that the first valve V1 in which the evaporation gas supplied in the refrigerant cycle RC is sent to the second pressure reducing device 420 is further provided . When the evaporated gas supplied to the refrigerant cycle RC is cooled by the second heat exchanger 120 and then sent to the second decompressor 420, the first valve V1 is supplied to the second heat exchanger 120 ) Is installed in the line to be sent to the second decompression device 420.

The first valve V1 receives a signal from the water level sensor 630 so that the level of the liquid droplet measured by the liquid level sensor 630 becomes the second set value or more, If it is likely to enter the decompression device 425, the flow of fluid is shut off to prevent fluid from entering the second decompression device 420. The second set value is larger than the first set value.

Unlike the first embodiment, the refrigerant cycle RC of the present embodiment further includes a bypass line BL and a second valve V2.

The bypass line BL allows the fluid used as the refrigerant in the second heat exchanger 120 to be bypassed to the fourth compressor 240 and the fifth compressor 245 after being reduced in pressure by the third decompression device 425 , And the second valve (V2) is installed in the bypass line (BL). When the fourth cooler 340 is installed downstream of the fourth compressor 240 and the fifth compressor 245, the bypass line BL is connected not only to the fourth compressor 240 and the fifth compressor 245, (340).

The second valve V2 receives a signal from the water level sensor 630 and opens when the level of the liquid droplet measured by the water level sensor 630 becomes the second set value or more. When the second valve V2 is opened, the fluid used as the refrigerant in the second heat exchanger 120 bypasses the fourth compressor 240 and the fifth compressor 245 along the bypass line BL.

That is, if the liquid level measured by the liquid level sensor 630 is equal to or higher than the second set value and there is a possibility that the liquid droplets may enter the second decompression device 420 or the third decompression device 425, V1 is closed to prevent fluid from flowing into the second decompression device 420 while the second valve V2 is opened so that the fluid bypasses the fourth compressor 240 and the fifth compressor 245, 240) and the fifth compressor (245).

Although not shown in FIG. 3, a valve is additionally provided in a line to which the fluid decompressed by the second decompressor 420 is sent to the third decompressor 425, so that the liquid measured by the water level sensor 630 The valve installed between the second pressure reducing device 420 and the third pressure reducing device 425 may be closed to prevent the droplet from flowing into the third pressure reducing device 425 when the enemy water level becomes equal to or higher than the second set value.

Further, a backflow prevention valve V3 may be installed downstream of the fourth compressor 240 and the fifth compressor 245 to prevent backflow of the fluid. When the fourth cooler 340 is installed downstream of the fourth compressor 240 and the fifth compressor 245, the backflow prevention valve V3 is installed downstream of the junction point of the bypass line BL, The valve V3 is installed downstream of the fourth cooler 340.

It will be apparent to those skilled in the art that various modifications and variations can be made in the present invention without departing from the spirit and scope of the invention. It is.

T: Storage tank RC: Refrigerant cycle
V1: first valve V2: second valve
V3: Reverse flow prevention valve BL: Bypass line
C1: 1st compander C2: 2nd compander
E: Fuel consumer 110: First heat exchanger
120: second heat exchanger 210: first compressor
220: second compressor 230: third compressor
240: fourth compressor 245: fifth compressor
310: first cooler 320: second cooler
330: third cooler 340: fourth cooler
410: First decompression device 420: Second decompression device
425: Third decompression device 500: Gas-liquid separator
610: Temperature sensor 615: Pressure sensor
620: Suction pipe 630: Water level sensor

Claims (20)

A first compressor for compressing the evaporation gas;
A second compressor installed in parallel with the first compressor for compressing other flows of evaporative gas not sent to the first compressor;
A first heat exchanger that cools the evaporated gas compressed by the first compressor or the second compressor by using heat as the refrigerant before the refrigerant is compressed by the first compressor or the second compressor;
A second heat exchanger for further cooling the fluid cooled by the first heat exchanger by using the evaporation gas circulating the refrigerant cycle as a refrigerant for further heat exchange; And
And a first decompression device for decompressing the fluid cooled by the second heat exchanger,
Wherein the refrigerant cycle includes:
A second decompression device for decompressing the evaporated gas supplied to the refrigerant cycle;
A third decompression device for further decompressing the fluid decompressed by the second decompression device; And
A fourth compressor and a fifth compressor compressing the fluid used as the refrigerant in the second heat exchanger after being reduced in pressure by the third decompressor;
A temperature sensor for measuring the temperature of the refrigerant circulating in the refrigerant cycle; And
And a pressure sensor for measuring a pressure of the refrigerant circulating in the refrigerant cycle,
The temperature measured by the temperature sensor is higher than the boiling point by a predetermined value (hereinafter, a temperature higher than the boiling point is referred to as a " third set value " ) Of the evaporation gas re-liquefaction system. The method according to claim 1,
Wherein the temperature sensor measures a temperature of a fluid provided downstream of the second decompressor and decompressed by the second decompressor,
Wherein the pressure sensor measures the pressure of the fluid which is provided downstream of the second pressure reducing device and reduced by the second pressure reducing device. The method of claim 2,
Wherein the flow rate of the third decompression device is reduced when the temperature measured by the temperature sensor becomes less than the third set value. The method according to any one of claims 1 to 3,
Wherein the fluid used as the refrigerant in the second heat exchanger is diverted into two flows and a portion thereof is supplied to the fourth compressor and the remainder is supplied to the fifth compressor. The method of claim 4,
Wherein the evaporation gas compressed by the fourth compressor and the evaporation gas compressed by the fifth compressor are combined and circulated in the refrigerant cycle. The method according to any one of claims 1 to 3,
Further comprising at least one suction pipe installed in the refrigerant cycle for collecting droplets contained in the fluid by gravity at a lower portion thereof. The method of claim 6,
The suction pipe
A line to which the fluid decompressed by the second decompression device is sent to the third decompression device; And
A line through which the fluid cooled by the second heat exchanger is sent to the second decompressor;
The evaporation gas re-liquefaction system for a ship. The method of claim 6,
And a water level sensor provided on the suction pipe,
And discharging droplets collected in the suction pipe when the level of the droplet measured by the water level sensor becomes a predetermined height or more. The method according to any one of claims 1 to 3,
Wherein one of the first compressor and the second compressor supplies the evaporation gas to the fuel demanding place (hereinafter, the compressor supplying the evaporation gas to the fuel consumption place is referred to as a 'fuel supplying compressor'),
The other compressor not supplying the evaporative gas to the fuel demanding place among the first compressor and the second compressor supplies the evaporative gas to the refrigerant cycle (hereinafter, the compressor supplying the refrigerant cycle evaporative gas is referred to as a 'compressor for refrigerant cycle' ), The evaporative gas re-liquefaction system for ships. The method of claim 9,
Wherein the refrigerant cycle includes at least one of the refrigerant cycle compressor, the second pressure reducing device, the third pressure reducing device, the second heat exchanger, the fourth compressor or the fifth compressor, To form a closed loop connecting the evaporation gas re-liquefaction system. The method of claim 9,
Wherein the evaporation gas supplied to the refrigerant cycle is cooled by the second heat exchanger and then sent to the second decompression device. The method of claim 11,
Wherein the refrigerant cycle includes at least one of the refrigerant cycle compressor, the second heat exchanger, the second decompressor, the third decompressor, the second heat exchanger, the fourth compressor or the fifth compressor, Thereby forming a closed loop connecting the compressor for the refrigerant cycle. The method according to any one of claims 1 to 3,
A third compressor for compressing the evaporated gas compressed by the first compressor or the second compressor and a third compressor for compressing the evaporated gas compressed by the first compressor or the second compressor, Further comprising a compressor. 14. The method of claim 13,
And the third compressor compresses the evaporation gas to 150 to 300 bar. 15. The method of claim 14,
And the third compressor compresses the evaporation gas to 150 to 170 bar. The method according to any one of claims 1 to 3,
Further comprising a gas-liquid separator provided downstream of the first decompression device for separating the re-liquefied liquefied gas and the vaporized gas remaining in a gaseous state. 18. The method of claim 16,
Wherein the evaporated gas separated by the gas-liquid separator is combined with the evaporated gas before being used as a refrigerant in the first heat exchanger and is used as a refrigerant in the first heat exchanger. 1) using evaporative gas as a refrigerant in a first heat exchanger;
2) splitting the evaporation gas used as the refrigerant of the first heat exchanger into two flows in the step 1);
3) sending the first flow to the first compressor and the remaining flow to the second compressor among the flows branched to the two flows in the step 2);
4) sending the evaporated gas compressed by the first compressor or the second compressor to the fuel consumer (hereinafter, the compressor supplying the evaporated gas to the fuel consumer is referred to as a 'fuel supply compressor');
5) The remaining evaporation gas not used in the fuel demanding place among the evaporation gases compressed by the 'fuel supply compressor' is used as the refrigerant in the evaporation gas supplied to the first heat exchanger in the step 1) Exchanging heat by a heat exchanger;
6) sending the evaporated gas compressed by other compressors other than the 'fuel supply compressor' among the first compressor and the second compressor to the refrigerant cycle (hereinafter, the compressor supplying the refrigerant cycle evaporated gas is referred to as' Compressor ');
7) cooling the fluid cooled by the first heat exchanger in the step 5) by heat exchange using the evaporator gas circulating in the refrigerant cycle as the refrigerant by the second heat exchanger; And
8) reducing the pressure of the fluid cooled by the second heat exchanger in the step 7)
The evaporation gas circulating through the refrigerant cycle is supplied to the evaporator
5-1) compressing the refrigerant by the refrigerant cycle compressor;
5-2) cooling by the second heat exchanger after being compressed in step 5-1);
5-3) After cooling in step 5-2), the pressure is reduced by the second pressure reducing device;
5-4) depressurizing in the step 5-3), and further depressurizing by the third decompressor;
5-5) using the refrigerant as a refrigerant in the second heat exchanger after further reducing the pressure in step 5-4); And
5-6) using the refrigerant as the refrigerant in the second heat exchanger in the step 5-5), then branching into two flows;
5-7) one of the two flows branched in the step 5-6) is sent to the fourth compressor and the remaining flow is sent to the fifth compressor; And
And 5-8) combining the evaporated gas compressed by the fourth compressor and the evaporated gas compressed by the fifth compressor,
The refrigerant circulating through the refrigerant cycle is heated to a temperature higher than the boiling point by a predetermined value (hereinafter, referred to as a third predetermined value), and the boiling point of the refrigerant circulating in the refrigerant cycle is calculated. ) Is maintained at a value equal to or greater than a predetermined value. 19. The method of claim 18,
Wherein the flow rate of the third decompression device is reduced when the temperature of the refrigerant circulating in the refrigerant cycle becomes less than the third set value. The method according to claim 18 or 19,
Wherein the droplets contained in the refrigerant circulating in the refrigerant cycle are collected at the lower portion of the suction pipe by gravity.

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