KR102274921B1 - Treatment system of gas - Google Patents

Abstract

A gas processing system according to an embodiment of the present invention, a vaporizer for vaporizing the liquefied gas stored in the liquefied gas storage tank through the vaporization fruit; a first heat exchanger for exchanging heat between the vaporized fruit and engine coolant; and a second heat exchanger for supplying a heat source to the vaporized fruit, wherein the first heat exchanger and the second heat exchanger supply a heat source to the vaporized fruit in the order of the first heat exchanger and the second heat exchanger do.

Description

Gas treatment system {Treatment system of gas}

The present invention relates to a gas treatment system.

A ship is a means of transport that carries a large amount of minerals, crude oil, natural gas, or thousands of containers or more and sails the ocean. It is made of steel and floats on the waterline due to buoyancy. move through

Such a ship generates thrust by driving an engine. At this time, the engine uses gasoline or diesel to move the piston so that the crankshaft is rotated by the reciprocating motion of the piston, so that the shaft connected to the crankshaft is rotated to drive the propeller It was common to do so.

However, recently, an LNG fuel supply method in which an engine is driven by using LNG as a fuel is used in an LNG carrier that transports liquefied natural gas. It is also applied to other ships.

In general, LNG is known to be a clean fuel and has more abundant reserves than petroleum, and its usage is rapidly increasing as mining and transport technologies are developed. In such LNG, methane, the main component, is generally stored in a liquid state by lowering the temperature to -162 degrees or less under 1 atm. The volume of liquefied methane is about 1/600 of the volume of gaseous methane, which is a standard state, and the specific gravity is 0.42, which is about one-half of the share of crude oil.

However, the temperature and pressure required to drive the consumer may be different from the state of the LNG stored in the tank. Therefore, in recent years, continuous research and development has been made on a technology for supplying the LNG stored in a liquid state by controlling the temperature and pressure, and the like.

In addition, when LNG is stored in liquid form, some of the LNG is vaporized and boil-off gas (BOG) is generated as heat penetrates into the tank. In the past, boil-off gas was used to reduce the tank pressure to remove the risk of damage to the tank. It was simply discharged to the outside. However, in recent years, the need for development of utilization measures such as re-liquefying the boil-off gas generated in the tank and supplying it to the customers is gradually increasing.

The present invention was created to solve the problems of the prior art as described above, and an object of the present invention is to provide a gas treatment system for effectively supplying liquefied gas and/or boil-off gas from a liquefied gas storage tank to a consumer.

A gas processing system according to the present invention includes: a vaporizer for vaporizing liquefied gas stored in a liquefied gas storage tank through vaporization fruit; a first heat exchanger for exchanging heat between the vaporized fruit and engine coolant; and a second heat exchanger for supplying a heat source to the vaporized fruit, wherein the first heat exchanger and the second heat exchanger supply a heat source to the vaporized fruit in the order of the first heat exchanger and the second heat exchanger do.

Specifically, further comprising a circulation pump circulating to supply the vaporized fruit to the vaporizer, wherein the first heat exchanger and the second heat exchanger are in series in the order of the circulation pump, the first heat exchanger, and the second heat exchanger can be connected

Specifically, further comprising a circulation pump circulating to supply the vaporized fruit to the vaporizer, wherein the first heat exchanger and the second heat exchanger are in series in the order of the first heat exchanger, the circulation pump, and the second heat exchanger can be connected

Specifically, the first heat exchanger and the second heat exchanger may have different types of heat exchangers.

Specifically, the first heat exchanger and the second heat exchanger may have the same type of heat exchanger.

Specifically, the second heat exchanger may use steam or seawater as a heat source supplied to the vaporized fruit.

Specifically, a first bypass line connecting the front end and the rear end of the first heat exchanger to bypass the vaporized fruit passing through the first heat exchanger from the rear end to the front end of the first heat exchanger; a second bypass line connecting the front end and the rear end of the second heat exchanger to bypass the vaporized fruit passing through the second heat exchanger from the rear end to the front end of the second heat exchanger; and a controller controlling the first bypass line or the second bypass line.

Specifically, when the vaporized fruit supplied to the vaporizer is less than or equal to a preset temperature value, the control unit may drive the first bypass line or the second bypass line to reheat the vaporized fruit.

Specifically, the preset temperature value may be 85 degrees to 95 degrees.

Specifically, the heat source may be supplied to the second heat exchanger depending on the heat source supply capability of the first heat exchanger.

The gas treatment system according to the present invention can increase system stability and reliability by effectively supplying liquefied gas and/or boil-off gas from a liquefied gas storage tank to a consumer.

1 is a conceptual diagram of a gas processing system according to an embodiment of the present invention.
2A is a conceptual diagram of a vaporization system in the gas processing system of the present invention.
2B is a conceptual diagram of a vaporization system in the gas processing system of the present invention.
2C is a conceptual diagram of a vaporization system in the gas processing system of the present invention.

The objects, specific advantages and novel features of the present invention will become more apparent from the following detailed description and preferred embodiments taken in conjunction with the accompanying drawings. In the present specification, in adding reference numbers to the components of each drawing, it should be noted that only the same components are given the same number as possible even though they are indicated on different drawings. In addition, in describing the present invention, if it is determined that a detailed description of a related known technology may unnecessarily obscure the subject matter of the present invention, the detailed description thereof will be omitted.

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

Hereinafter, the liquefied gas may be LPG, LNG, ethane, etc., for example, may mean LNG (Liquefied Natural Gas), and the boil-off gas may mean BOG (Boil Off Gas) such as naturally vaporized LNG.

Liquefied gas may be referred to regardless of a change in state, such as a liquid state, a gaseous state, a liquid and gas mixture state, a supercooled state, a supercritical state, etc. Note that the same applies to boil-off gas. In addition, in the present invention, the processing target is not limited to liquefied gas, and may be a liquefied gas processing system and/or a boil-off gas processing system.

1 is a conceptual diagram of a gas processing system according to an embodiment of the present invention.

Referring to FIG. 1 , the gas treatment system according to an embodiment of the present invention may be mounted on a ship such as an LNG carrier, and includes a liquefied gas storage tank 10 , a consumer 20 , a boil-off gas compressor 30 , It includes a boosting pump 40 , a high pressure pump 41 , a carburetor 42 , and a forced carburetor 50 .

Hereinafter, each configuration of the gas processing system 1 according to an embodiment of the present invention will be described, and after the configuration description is completed, each embodiment will be described through a relationship between the configurations of the system.

In an embodiment of the present invention, first to thirteenth lines L1 to L13 may be further included. Valves (not shown) capable of adjusting the opening degree may be installed in each line, and the supply amount of boil-off gas and/or liquefied gas and/or various refrigerants may be controlled according to the control of the opening degree of each valve.

The liquefied gas storage tank 10 may store liquefied gas of -163 degrees. The liquefied gas storage tank 10 may be a tank such as a stand-alone type, a membrane type, a pressurized type, etc., and if it can store liquefied gas, the size, shape, structure, etc. are not particularly limited.

In the liquefied gas storage tank 10, liquefied gas in a liquid state and boil-off gas in a gaseous state may be mixed. This is because, as external heat penetrates into the liquefied gas storage tank 10 and the liquefied gas is heated, boil-off gas may be generated.

At this time, since the boil-off gas causes an increase in the internal pressure of the liquefied gas storage tank 10 as the flow rate increases, discharge is preferable for the protection of the liquefied gas storage tank 10 . Therefore, the present invention can properly discharge boil-off gas according to the pressure of the liquefied gas storage tank (10).

The discharged BOG may be burned and discarded by a gas combustion unit 23, which will be described later, or may be supplied to and consumed by a consumer 20 (engine, turbine, boiler, etc.).

Alternatively, the BOG discharged from the liquefied gas storage tank 10 is cooled to below the boiling point by a re-liquefaction device 37, etc., which will be described later, and then liquefied from a gaseous state to a liquid state (the same as liquefied gas as liquefied BOG/ Similarly) may be processed such as returning to the liquefied gas storage tank (10).

The liquefied gas storage tank 10 may include a heat insulating part and a barrier part to prevent penetration of external heat.

The barrier portion may be provided on the inner side (the side adjacent to the liquefied gas) relative to the heat insulating portion, and the heat insulation portion may be provided on the outer side (the side adjacent to the hull) relative to the barrier portion. However, this may vary depending on the structure of the liquefied gas storage tank 10, and may be variously determined depending on whether the liquefied gas storage tank 10 is a membrane type, an independent type, a pressurized type, or the like.

The heat insulating part insulates the inside and the outside of the liquefied gas storage tank 10 using a heat insulating material. The heat insulating part forms a heat insulating structure using various heat insulating materials such as polyurethane foam (PUF), perlite, and wood, and may include a metal such as stainless steel (SUS) or INVAR.

When the liquefied gas storage tank 10 is a membrane type, the structure may be determined according to a conventionally well-known type such as Mark III, No. 96, etc., when the liquefied gas storage tank 10 is a standalone type, MOSS, SPB, etc. The structure may be determined according to a conventionally well-known type of . Of course, the structure of the heat insulating unit is not limited to the above example.

The barrier part may insulate the inside and the outside of the liquefied gas storage tank 10 using an inert gas. The barrier part may form an empty space, and the empty space of the barrier part may be formed between the inner wall of the liquefied gas storage tank 10 and the heat insulating part, and/or between the outer wall of the liquefied gas storage tank 10 and the heat insulating part, etc. .

The barrier part may be filled with an inert gas such as nitrogen, and the inert gas may be supplied by an inert gas supplier provided outside. In this case, the inert gas supplier may use a nitrogen generator (N2 generator).

The consumer 20 may be a configuration that consumes liquefied gas or the like (liquefied gas, boil-off gas, or flash gas), and generates or burns energy while consuming liquefied gas or the like.

As an example, the customer 20 is a low-pressure customer using liquefied gas having a pressure of about 1 bar to 10 bar (absolute pressure), such as a turbine low-pressure engine (DFDE, DFDG, XDF, etc.), a re-liquefaction device, a boiler, a gas combustion device, etc. It may be a high-pressure demander using liquefied gas having a pressure of about 200bar to 400bar (absolute pressure), such as a high-pressure engine (ME-GI engine, etc.), and the pressure of the liquefied gas required for each consumer 20 may be different.

That is, in the present invention, the consumer 20 refers to all configurations that consume liquefied gas and the like, and the present invention does not limit the consumer 20 to a specific configuration.

In the embodiment of the present invention, it has a configuration of a gas supply unit for processing the liquefied gas or boil-off gas stored in the liquefied gas storage tank (10). Here, the gas supply unit is a configuration for delivering liquefied gas and/or boil-off gas to a consumer 20 such as an engine, and includes a boil-off gas compressor 30, a boosting pump 40, a high-pressure pump 41, a vaporizer 42, and the like. may include

The boil-off gas compressor 30 compresses the boil-off gas discharged from the liquefied gas storage tank 10 . The BOG compressor 30 may be of a centrifugal type, a reciprocating type, or the like, and a plurality of BOG compressors 30 may constitute a BOG compression unit (not shown).

In this case, the plurality of BOG compressors 30 constituting the BOG compression unit may be provided so that all of them are of a centrifugal type, all of a reciprocating type, or a mixture of a centrifugal type and a reciprocating type.

For example, the boil-off gas compressor 30 includes a reciprocating compressor and/or a centrifugal compressor, and the reciprocating compressor and the centrifugal compressor may be provided in parallel, and the discharge pressure of the reciprocating compressor and the centrifugal compressor is may be the same or different.

For example, in the present invention, the boil-off gas compressor 30 may be of a centrifugal type, and may be configured in two stages, three stages, five stages, six stages, and the like. Each stage is compressed according to the requirements of the boil-off gas to be supplied only according to the type of the customer 20 , but it does not indicate that the larger the stage number, the relatively high the discharge pressure.

In addition, the BOG compressor 30 may be configured as a cryogenic compressor in order to process BOG in a low temperature state of about -100 degrees Celsius discharged from the liquefied gas storage tank 10 . However, when the BOG is compressed by the BOG compressor 30, the temperature of BOG may rise. Therefore, some BOG compressors upstream among the multi-stage BOG compressors included in the BOG compression unit are cryogenic compressors. , the remaining BOG compressor downstream may be a compressor for room temperature.

When the temperature of the boil-off gas increases while the boil-off gas is compressed by the boil-off gas compressor 30, the volume of the boil-off gas may increase as the volume of the boil-off gas increases together. This may cause an unnecessary load increase of the BOG compressor 30 , and at least one BOG compressor 30 upstream and/or at least one BOG compressor 30 downstream of the compressed evaporation gas compressor 30 . A boil-off gas cooler (not shown) for cooling the gas may be provided.

The boil-off gas cooler can cool the boil-off gas using various cooling heat sources. For example, the boil-off gas cooler uses seawater, the re-liquefaction refrigerant of the re-liquefaction device 37, liquefied gas, boil-off gas, flash gas, etc. in various ways. Can be used.

A buffer tank (not shown) in addition to the BOG cooler may be provided between each stage of the BOG compressor 30 . The buffer tank may be provided to continuously supply the boil-off gas introduced into each stage of the boil-off gas compressor 30 and to maintain a constant supply pressure.

BOG flowing into the BOG compressor 30 may be heat-exchanged with the compressed BOG. However, the BOG introduced into the BOG compressor 30 due to heat exchange may be preheated, and thus the BOG compressor 30 may all be configured as a compressor for room temperature.

The BOG compressor 30 may compress BOG to about 10 bar (absolute pressure) to 400 bar (absolute pressure). This may vary depending on where the boil-off gas discharged from the boil-off gas compressor 30 is used.

For example, when the BOG compressed in the BOG compressor 30 is used for a low-pressure consumer 22 such as a turbine, a low-pressure engine (DFDE, DFDG, XDF, etc.), a reliquefaction device, a boiler, or a gas combustion device, the compressed BOG is The pressure may be about 1 bar to 10 bar (absolute pressure), and when the compressed BOG is used in a high-pressure demander 21 such as a high-pressure engine (ME-GI, etc.), the pressure of the compressed BOG is about 200 bar to 400 bar (absolute pressure). ) can be

Of course, the BOG compressor 30 is provided in multiple stages, and BOG compressed to a low pressure by some BOG compressors 30 is discharged to the outside of the BOG compressor 30 to be used in the low-pressure demand 22 . In addition, the BOG further compressed to a high pressure by the remaining BOG compressor 30 is discharged to the outside of the BOG compressor 30 to be used in the high-pressure consumer 21 .

That is, in the BOG compression unit having the BOG compressor 30 provided in multiple stages, the pressure of BOG supplied to each consumer 20, the number of BOG compressors 30, the degree of multi-stage compression of BOG, etc. It is not limited and may be variously determined.

In order to deliver BOG from the liquefied gas storage tank 10 through the BOG compressor 30 to the low-pressure consumer 22 or the high-pressure consumer 21, from the liquefied gas storage tank 10 to each consumer 20 is supplied. Lines (second, third, fifth, seventh, eighth lines L2, L3, L5, L7, L8, etc.) may be provided.

At this time, the supply line connected from the BOG compressor (end or middle end, etc.) to the low pressure demander 22 may be a low pressure supply line (the third line (L3)), and the BOG compressor 30 (end or middle end, etc.) A supply line connected from the to the high-pressure demander 21 may be a high-pressure supply line (the second line L2). Accordingly, the supply line may be branched into a low pressure supply line (the third line L3) and a high pressure supply line (the second line L2) based on the BOG compressor 30 .

BOG compressor 30, BOG is compressed to a low pressure through only a portion of BOG compressors 30 provided in multiple stages, and is supplied to the low pressure demander 22 along the low pressure supply line L3, and is provided in multiple stages. After passing through all of the BOG compressors 30, BOG is compressed to a high pressure and may be supplied to the high-pressure consumer 21 along the high-pressure supply line L2.

BOG compressor 30, some may not use lubricating oil, the rest may use lubricating oil. For example, if the BOG compressor 30 is provided in five stages, the BOG compressors of stages 1 to 3 do not use lubricating oil (lubricating oil is not mixed in the BOG), and stages 4 to 5 use lubricating oil. (lubricating oil is mixed into boil-off gas). This is because, in the case of the high-pressure stage, lubricating oil is required to smoothly drive the piston of the boil-off gas compressor 30 as the pressure of the boil-off gas changes to a high pressure.

Of course, the number of BOG compressors 30 is not limited to the above, and a part of the front end (low pressure end) of the plurality of BOG compressors 30 does not use lubricating oil, and the rest of the rear end (high pressure end) may use lubricating oil. .

The first pressure reducing valve 341 may reduce or expand the boil-off gas to be supplied to the reliquefaction apparatus 37 by being pressurized by the boil-off gas compressor 30 . Although not shown here, the first pressure reducing valve 341 depressurizes or expands the boil-off gas pressurized in the boil-off gas compressor 30 to supply not only the reliquefaction apparatus 37 but also the gas combustion apparatus 23, etc. .

The first pressure reducing valve 341 may be provided together with the second pressure reducing valve 342 to depressurize or expand the boil-off gas pressurized in the boil-off gas compressor 30 in multiple stages. For example, the first pressure reducing valve 341 may re-press the boil-off gas pressurized in the boil-off gas compressor 30 or the boil-off gas branched and supplied to the intermediate stage of the boil-off gas compressor 30 after first decompression or first expansion. BOG supplied to the liquefaction device 37 and heat-exchanged in the reliquefaction device 37 may be reliquefied by secondary pressure reduction or secondary expansion through the second pressure reducing valve 342 again.

The above-described techniques of the first pressure reducing valve 341 may be implemented by changing the configuration for each embodiment.

The gas-liquid separator 35 separates gas from the boil-off gas reduced or expanded by the first pressure reducing valve 341 or the second pressure reducing valve 342 . BOG is separated into liquid and gas in the gas-liquid separator 35 , and the liquid is supplied to the liquefied gas storage tank 10 , and the gas may be supplied to the gas combustion device 23 as a flash gas.

Here, the boil-off gas supplied to the gas-liquid separator 35 may be in a cooled state by being reduced in pressure by the first pressure reducing valve 341 or the second pressure reducing valve 342 . For example, in the boil-off gas compressor 30, the boil-off gas may be pressurized in multiple stages to have a pressure of 200 bar to 400 bar, and the temperature may be made around 45 degrees. BOG, which has risen to a temperature of about 45 degrees, is recovered to the reliquefaction device 37 through the first pressure reducing valve 341, and the BOG heat-exchanged in the reliquefaction device 37 is again returned to the second pressure reducing valve 342. is supplied with At this time, the boil-off gas in the first pressure reducing valve 341 or the second pressure reducing valve 342 may be cooled by reduced pressure to have a pressure of about 1 bar and a temperature of about -162.3 degrees.

As described above, in this embodiment, the boil-off gas supplied to the gas-liquid separator 35 is decompressed (or multi-stage decompression) at the first pressure reducing valve 341 or the second pressure reducing valve 342 to have a temperature lower than -162 degrees. , about 30-40% of the boil-off gas can be liquefied. After that, the gas-liquid separator 35 recovers the liquefied gas to the liquefied gas storage tank 10, and does not discard the flash gas generated in the gas-liquid separator 35, but through the ninth line L9, the gas combustion device 232. can be supplied and burned.

The second pressure reducing valve 342 depressurizes or expands the boil-off gas pressurized by the boil-off gas compressor 30 and heat-exchanged in the re-liquefaction device 37 to liquefy at least a part thereof. For example, the second pressure reducing valve 342 may reduce the boil-off gas pressure to 1 bar to 10 bar, and when the boil-off gas is liquefied and transferred to the liquefied gas storage tank 10, the pressure may be reduced to even 1 bar, and when the pressure is reduced, the boil-off gas may be reduced. can have a cooling effect.

Here, the BOG pressurized by the BOG compressor 30 is cooled by heat exchange with the BOG supplied from the liquefied gas storage tank 10 in the reliquefaction device 37, but the pressure is discharged from the BOG compressor 30. The discharge pressure can be maintained. In the present embodiment, the boil-off gas may be liquefied by depressurizing the boil-off gas using the second pressure reducing valve 342 to cool the boil-off gas. In this case, as the pressure range to be reduced is larger, the cooling effect of the BOG may be increased. For example, the second pressure reducing valve 342 may reduce the BOG pressurized to 300 bar by the BOG compressor 30 to 1 bar.

The second pressure reducing valve 342 may be a Joule Thompson valve. Alternatively, the second pressure reducing valve 342 may be formed of an expander (not shown). In the case of the Joule Thompson valve, it is possible to effectively cool the BOG through reduced pressure so that at least a part of the BOG is liquefied. In this case, the expander may also be configured as an expander (not shown).

On the other hand, the expander can be driven without using separate power, and in particular, the efficiency of the gas treatment system 1 can be improved by using the generated power as power for driving the BOG compressor 30 . Power transmission may be performed, for example, by gear connection or transmission after electrical conversion.

The second pressure reducing valve 342, together with the above-described first pressure reducing valve 341, pressurizes the boil-off gas pressurized in the boil-off gas compressor 30 and heat-exchanged in the reliquefaction device 37 in multiple stages, or a boil-off gas compressor. (30) It is possible to depressurize the boil-off gas branched and supplied to the intermediate stage in multiple stages, which can be flexibly applied by changing the configuration according to each embodiment.

The boosting pump 40 and the high pressure pump 41 may pressurize the liquefied gas to or close to the pressure required by the demander 20 . In the present invention, the demand 20, the high-pressure demand 21 and the low-pressure demand 22, etc. may be, since the pressure of the liquefied gas required for each demand 20 may be different, as mentioned above, the boosting pump 40 ) and the high-pressure pump 41, or only the boosting pump 40, or only the high-pressure pump 41, may be provided in various other ways. That is, the pressure of the liquefied gas pressurized by the pumps 40 and 41 may be variously determined from 10 bar to 400 bar (absolute pressure) according to the required pressure of the demand 20, and the present invention is not particularly limited thereto.

At this time, each of the boosting pump 40 and the high-pressure pump 41 may be provided in plurality, and one pump may be used as a main and the other pump may be used as a backup. Of course, two or more pumps can be driven simultaneously to lower the load.

Lines (first and sixth lines; L1, L6, etc.) for supplying liquefied gas from the liquefied gas storage tank 10 to the pumps 40 and 41 may be connected, and may flow along the lines L1 and L6. can At this time, the lines L1 and L6 for supplying the liquefied gas are connected to the vaporizer 42 and/or the demand 20 to be described later so that the liquefied gas is delivered from the liquefied gas storage tank 10 to the demand 20. have.

Lines L1 and L6 for supplying liquefied gas are high-pressure liquefied gas supply lines (first line; L1) connected from the liquefied gas storage tank 10 to the high-pressure demander 21 via pumps 40 and 41 . and/or it may be a low-pressure liquefied gas supply line (sixth line; L6) connected from the liquefied gas storage tank 10 to the low-pressure consumer 22 via the pump 40 . When the high-pressure liquefied gas supply line (L1) and the low-pressure liquefied gas supply line (L6) are provided at the same time, the high-pressure liquefied gas supply line (L1) and the low-pressure liquefied gas supply line (L6) are branched from one liquefied gas supply line. and the branch point may be variously determined according to the required pressure of the demander 20. (For example, between the boosting pump 40 and the high pressure pump 41, etc.)

The vaporizer 42 heats the liquefied gas. The liquefied gas stored in the liquefied gas storage tank 10 is a cryogenic temperature of about -160 degrees, and the required temperature of the liquefied gas required by the demand 20 may be 10 to 50 degrees (preferably about 45 degrees). Therefore, when the liquefied gas is to be delivered to the consumer 20, a temperature increase of the liquefied gas is required.

Of course, when the liquefied gas is pressurized with the pumps 40 and 41, the temperature of the liquefied gas may rise, but this is not sufficient, so the carburetor 42 uses the liquefied gas as a separate heat source (steam, glycol water, seawater, engine It can be heated using exhaust, engine coolant, electricity, etc.).

In order to supply a heat source to the vaporizer 42 , the present invention may include a vaporized fruit storage tank 421 , a vaporized fruit circulation pump 422 , a vaporized fruit supply device 423 , and a vaporized heat exchanger 424 .

The vaporized fruit storage tank 421 is a tank that temporarily stores the vaporized fruit as a heat source, and can stably maintain the supply amount of the vaporized fruit.

The vaporized fruit circulation pump 422 is configured to supply vaporized fruits from the vaporized fruit storage tank 421 to the vaporized heat exchanger 424, and a plurality of vaporized fruits may be provided in parallel or connected in series, and when the vaporized fruits are gas, A heat source compressor (not shown) may be provided in place of the vaporized fruit circulation pump 422 .

The vaporized fruit supply device 423 heats the vaporized fruit. Since the vaporized fruit may be cooled while heating the liquefied gas in the vaporization heat exchanger 424, it is necessary to supplement heat to the cooled vaporized fruit. Accordingly, the vaporized fruit may be heated by steam or the like, and then the liquefied gas may be heated in the vaporization heat exchanger 424 .

The vaporized fruit supply device 423 may include a plurality of vaporized fruit first supply device 4231 and a vaporized fruit second supply device 4232 . Here, the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232 may be engine cooling water (Jacket Cooling Water) or seawater, respectively, and may be configured in parallel or in series with each other.

At this time, the vaporized fruit flows along the vaporized fruit circulation line (GL) that circulates and connects the vaporized heat exchanger 424, the vaporized fruit supply device 423, the vaporized fruit circulation pump 422, and the vaporized fruit storage tank 421. However, each configuration connected by the vaporized fruit circulation line (GL) (evaporated heat exchanger 424, vaporized fruit supply device 423, vaporized fruit circulation pump 422, and vaporized fruit storage tank 421) Unlike the drawings, the order of may be variously changed.

In addition, in the vaporized fruit circulation line (GL), the vaporized fruit branch line (GLb, GBL1, GBL2) to bypass the vaporized fruit supply device 423 and appropriately adjust the temperature of the vaporized fruit supplied to the vaporized heat exchanger 424 ) can be connected, and the vaporized fruit branch lines GLb, GBL1, GBL2 are branched from the vaporized fruit circulation line GL upstream of the vaporized fruit supply device 423 and the vaporized fruit supply device 423 downstream of the vaporized fruit supply device 423. It may be integrated into the circulation line GL.

The vaporization heat exchanger 424 may supply a heat source to the liquefied gas flowing on the liquefied gas supply line L1 through the circulating vaporization fruit to vaporize the liquefied gas. The configuration type of the vaporization heat exchanger 424 may employ various configurations of other heat exchangers such as shell & tube, and is not specifically limited.

The gas supply unit may further include a forced vaporizer 50 , a gas-liquid separator 51 , and a heater 52 . At this time, the forced vaporizer 50, the gas-liquid separator 51, and the heater 52 are low-pressure liquefied gas supply configurations provided in the low-pressure liquefied gas supply line (the sixth line L6), and the above-described boosting and high-pressure pump 40 , 41), the vaporizer 42 may be a high-pressure liquefied gas supply configuration provided in the high-pressure liquefied gas supply line (L1).

The low-pressure liquefied gas supply configuration may be provided alone or together with the high-pressure liquefied gas supply configuration, and this is not particularly limited because it may vary according to the configuration of the demander 20 .

The low-pressure liquefied gas supply configuration and the high-pressure liquefied gas supply configuration may share the boosting pump 40 . That is, at least a portion of the low-pressure liquefied gas supply line and the high-pressure liquefied gas supply line is shared and may be branched downstream of the boosting pump 40 .

The forced vaporizer 50 vaporizes liquefied gas. The forced vaporizer 50 may receive the liquefied gas from the liquefied gas storage tank 10 and/or the boosting pump 40 and heat it using a heat source to vaporize it, and the heat source used at this time is as described in the vaporizer 42 above. Such as steam, glycol water, seawater, engine exhaust, engine coolant, electricity, and the like. The forced vaporizer 50 may also share a heat source with the vaporizer 42 .

The forced vaporizer 50 may be connected to the low-pressure liquefied gas supply line L6 , vaporize the liquefied gas and deliver it to the low-pressure demand 22 . At this time, methane, propane, butane, etc. are mixed in the liquefied gas. In the liquefied gas heated by the forced vaporizer 50, methane is vaporized, and propane or butane (hereinafter referred to as heavy carbon) can maintain a liquid phase.

The gas-liquid separator 51 (or may be a heavy carbon separator) separates the heavy carbon remaining in the liquid phase from the vaporized liquefied gas. When a large amount of heavy carbon is introduced into the consumer 20 (preferably the low-pressure consumer 22) that consumes the liquefied gas, the driving efficiency may be lowered. Therefore, in the present invention, by separating the heavy carbon that vaporizes the liquefied gas and maintains the liquid phase, the quality of the liquefied gas supplied to the consumer 20 can be improved, thereby increasing the driving efficiency of the consumer 20 .

At this time, the gas-liquid separator 51 may be referred to as a mist separator, a heavy carbon separator, etc., and the liquid heavy carbon may be returned to the liquefied gas storage tank 10 or delivered to a separately provided tank, for this purpose The separator 51 may be provided with a heavy carbon return line (not shown) connected to the liquefied gas storage tank 10 .

The heater 52 heats the liquefied gas from which the heavy carbon was separated. The forced vaporizer 50 heats the liquefied gas, but the vaporized liquefied gas has a temperature (for example, -100 degrees) for remaining in the liquid phase, so it may not reach the temperature required by the consumer 20 .

Accordingly, the heater 52 may heat the liquefied gas using a variety of heat sources similar to the forced vaporizer 50 , in which case the heat source may be shared with the forced vaporizer 50 and/or the vaporizer 42 .

In order to filter the liquefied gas flowing into the forced vaporizer 50 in the embodiment of the present invention, a strainer (not shown) may be further provided upstream of the forced vaporizer 50 . The strainer may be a combination of a plurality of valves and filters.

Although the liquefied gas is stored in the liquefied gas storage tank 10, foreign substances may be mixed in the liquefied gas inside the liquefied gas storage tank 10 by various fluids returned from the outside. Accordingly, the strainer may filter out foreign substances mixed in the liquefied gas, and allow the pure liquefied gas to be transferred to the forced vaporizer 50 .

The forced vaporizer 50 vaporizes the liquefied gas at about -100 degrees, which is to remove the heavy carbon as described above. At this time, the forced vaporizer 50 is provided with a liquefied gas regulator (not shown), and the state (temperature, etc.) of the liquefied gas transferred from the forced vaporizer 50 to the heavy carbon separator and/or the heater 52 can be adjusted. .

The gas supply unit in this embodiment may further include an H/D compressor 36 , a reliquefaction device 37 , and a return pump 38 .

The H/D compressor 36 may be used to compress the boil-off gas generated in the liquefied gas storage tank 10 during bunkering to the outside or to be incinerated, and the type of the compressor is not limited.

The re-liquefaction apparatus 37 may re-liquefy the excess boil-off gas through the re-liquefaction refrigerant to return it to the liquefied gas storage tank 10 . The reliquefaction apparatus 37 may include a reliquefaction heat exchanger (not shown) and a reliquefaction refrigerant supply device (not shown).

The re-liquefaction apparatus 37 supplies cooling heat to re-liquefy the boil-off gas through the re-liquefaction refrigerant supply apparatus, and the refrigerant supplied from the re-liquefaction refrigerant supply apparatus is transferred to the re-liquefaction heat exchanger through a separate pump (not shown). It can be supplied and reliquefied by supplying cooling heat to the boil-off gas.

The return pump 38 transfers the liquid phase to the liquefied gas storage tank 10 through the tenth line L10 in the gas-liquid separator 35 that separates the boil-off gas reliquefied in the reliquefaction device 37 into a liquid phase and a gas phase. can supply

At this time, in the present invention, when the liquid phase is not supplied from the gas-liquid separator 35 to the liquefied gas storage tank 10 (due to the pressure difference between the gas-liquid separator 35 and the internal pressure of the liquefied gas storage tank 10), the supply of the liquid is stopped), the liquid phase of the gas-liquid separator 35 is supplied to the liquefied gas storage tank 10 through the bypass line 11th line L11 and bypass valves (not shown) and the return pump 38 . can

Specifically, when the liquid boil-off gas stored in the gas-liquid separator 35 is stored at a pressure greater than the internal pressure of the liquefied gas storage tank 10, it is supplied to the liquefied gas storage tank 10 through the tenth line L10. If the liquid boil-off gas stored in the first gas-liquid separator 35 is stored at a pressure smaller than the internal pressure of the liquefied gas storage tank 10, the re-liquefaction supply pump 38 is driven to drive the liquefied gas storage tank ( 10) can be supplied.

Hereinafter, embodiments of the gas processing system that can be derived through each configuration described above will be described.

The gas processing system 1 according to the embodiment of the present invention may further include a configuration for processing liquefied gas or boil-off gas through the individual configurations described above and supplying the liquefied gas or boil-off gas to the consumer 20 .

Hereinafter, the processing mechanism of the liquefied gas stored in the liquefied gas storage tank 10 and the processing mechanism of the boil-off gas generated in the liquefied gas storage tank 10 will be described in detail below.

First, looking at the processing mechanism of the liquefied gas stored in the liquefied gas storage tank 10, the gas processing system 1 according to the embodiment of the present invention uses the liquefied gas stored in the liquefied gas storage tank 10 in the first line L1. ) while supplying it to the consumer 20, using the boosting pump 40 to first pressurize it, and then filter the impurities in the liquefied gas through a strainer (not shown), and then a) the sixth line (L6) Accordingly, it may be supplied to the forced vaporizer 50 or b) may be supplied to the high-pressure pump 41 along the first line L1.

a) The liquefied gas supplied to the forced vaporizer 50 along the sixth line L6 is heated through the forced vaporizer 50 and is at least partially vaporized, and the forced vaporized liquefied gas is supplied to the gas-liquid separator 51 . is separated into gas and liquid, and as the gas and liquid are separated, the heavy carbon is separated into a liquid and returned to the liquefied gas storage tank 10, and the gas from which the heavy carbon component is removed can be supplied to the low-pressure consumer 22. .

b) The liquefied gas supplied to the high-pressure pump 41 along the first line L1 is pressurized to a high pressure by the high-pressure pump 41, vaporized by the vaporizer 42, and then supplied to the high-pressure consumer 21. can

Looking at the processing mechanism of the boil-off gas generated in the liquefied gas storage tank 10, the gas processing system 1 according to the embodiment of the present invention c) the second boil-off gas generated in the liquefied gas storage tank 10 Line (L2) or d) along the third line (L3) by using the boil-off gas compressor (30) can be supplied to the demand (20) by multi-stage pressurization.

c) BOG supplied through the second line L2 may be compressed in multiple stages by the BOG compressor 30 at high pressure and supplied to the high-pressure consumer 21, and the high pressure through the process b) described above. The vaporized liquefied gas may also be joined and supplied to the high-pressure consumer 21 together.

d) BOG supplied through the third line L3 is BOG supplied by branching from the second or third stage of the BOG compressor 30 and supplied through the second line L2, It may be supplied to the low-pressure consumer 22 , and may also be supplied to the low-pressure demand 22 by joining with the liquefied gas forcibly vaporized through the process of a) described above.

At this time, the forcibly vaporized liquefied gas supplied through the forced vaporizer 50 may be supplied when the fuel consumption of the low-pressure demander 22 increases, and of course, is not limited to this example. (The liquefied gas stored in the liquefied gas storage tank 10 has a high proportion of heavy carbon, so in order to lower it, a forced vaporizer 50 and a gas-liquid separator 51 are used to liquefy the heavy carbon, and only the gas from which it is removed is a low-pressure consumer 22 ), so that the efficiency of the low-pressure demander 22 is increased.)

Of course, the boil-off gas generated in the liquefied gas storage tank 10 may be supplied to the gas combustion device 23 and the vent mast 24 as described above, and in this case, through a separate line (not shown) It may be supplied to the gas combustion device 23 or the vent mast 24 through a valve (not shown) provided on the line.

The gas processing system 1 according to the embodiment of the present invention may include a technology for accumulating the liquefied gas storage tank 10 .

BOG generated in the liquefied gas storage tank 10 of the embodiment of the present invention is supplied to the BOG consumer 20 when the internal pressure of the liquefied gas storage tank 10 is equal to or greater than a preset pressure, and the liquefied gas storage tank 10 ) is accumulating inside the liquefied gas storage tank 10 when the internal pressure is less than the preset pressure. Here, the preset pressure may be 1.06 bar to 1.12 bar, and the boil-off gas consumer 20 includes a gas combustion device 23 and a vent mast 24, and the internal pressure of the liquefied gas storage tank 10 is When the pressure is less than the set pressure, the driving of the engine 20 that generates the propulsion force of the ship (not shown) is stopped, or may be a case of bunkering, anchoring, or ballast voting.

Specifically, in the embodiment of the present invention, when the internal pressure of the liquefied gas storage tank 10 is less than the preset pressure, the operation of the boil-off gas compressor 30 is stopped, and the boil-off gas generated from the liquefied gas storage tank 10 is stopped. can be stored as it is in the liquefied gas storage tank (10).

In an embodiment of the present invention, when the internal pressure of the liquefied gas storage tank 10 is equal to or greater than the preset pressure, more specifically, when the internal pressure of the liquefied gas storage tank 10 is 1.17 bar to 1.20 bar, the liquefied gas storage tank The boil-off gas generated in (10) is pressurized in the boil-off gas compressor (30) and supplied to the gas combustion device (23) that burns the boil-off gas, and the internal pressure of the liquefied gas storage tank (10) is 1.20 bar to 1.25 bar. In this case, the boil-off gas generated in the liquefied gas storage tank 10 is supplied to a vent mast and discharged to the outside, and when the internal pressure of the liquefied gas storage tank 10 is 1.25 bar or more, the liquefied gas storage tank ( The boil-off gas generated in 10) may be supplied to a safety valve (not shown; safety valve) and discharged from the inside of the liquefied gas storage tank 10 to the outside through the safety valve.

As described above, in the embodiment of the present invention, by accumulating the boil-off gas generated in the liquefied gas storage tank 10 to within a preset pressure, it is necessary to operate the boil-off gas compressor 30 to discharge and burn the boil-off gas to the outside. Electricity consumption can be reduced because there is no evaporator, and since the boil-off gas is not emitted to the outside, there is an effect of preventing the wastage of the boil-off gas.

The gas treatment system 1 according to the embodiment of the present invention may include a technology for using the H/D compressor 36 in common during bunkering and maintenance of the liquefied gas storage tank 10 .

In the gas processing system 1 according to the embodiment of the present invention, the H/D compressor 36 for pressurizing the boil-off gas generated in the liquefied gas storage tank 10, the evaporation compressed by the H/D compressor 36 A heater (not shown) that heats gas and a shore storage (Shore) in which liquefied gas to be supplied to the liquefied gas storage tank 10 during bunkering is stored, or for temporarily storing boil-off gas generated from the liquefied gas storage tank 10 during bunkering. Temporary storage (not shown) is included as a main component.

In the case of loading liquefied gas from the outside into the liquefied gas storage tank 10 for the first time (including the case of loading liquefied gas after completing the maintenance work of the liquefied gas storage tank 10), that is, during bunkering, liquefied gas Considering that is a cryogenic ignitable material, a special operation different from that of a general storage tank, that is, a replacement operation, must be preceded.

In general, the replacement method of the liquefied gas storage tank 10 is to supply dry gas to the inside of the liquefied gas storage tank 10 to remove moisture, and inert gas to the liquefied gas storage tank 10 to eliminate the possibility of fire or explosion. ) to remove oxygen by supplying it to the inside. Thereafter, a hydrocarbon gas is supplied to the inside of the liquefied gas storage tank 10 to remove the inert gas, and a cool-down process of cooling the liquefied gas storage tank 10 using the liquefied gas is performed. . When the cool-down process is completed, the replacement method is completed, and only after that, liquefied gas such as LNG is supplied to the inside of the liquefied gas storage tank 10 to perform the shipping operation.

Conversely, in the case of unloading the liquefied gas stored in the liquefied gas storage tank 10 to the shore (including the case of removing all the liquefied gas before maintenance of the liquefied gas storage tank 10), , the process is slightly different from the process described above.

First, all of the liquefied gas stored in the liquefied gas storage tank 10 is discharged to the demand (Shore). At this time, residual liquefied gas is present, and a warm-up step is performed to remove all of the remaining liquefied gas. The warm-up step increases the internal temperature of the liquefied gas storage tank 10 by compressing the boil-off gas generated in the liquefied gas storage tank 10 with a compressor, heating it with a separate heater, and returning it to the liquefied gas storage tank 10 again. Allow all remaining liquefied gas to vaporize. After the warm-up step, an inert gas is supplied to remove all of the boil-off gas remaining in the liquefied gas storage tank 10, a drying gas is input to dry the inside, and then oxygen is supplied so that air is supplied to the inside. By going through the above process, the unloading process of the liquefied gas storage tank 10 is completed, and a worker for performing maintenance work and the like can be drawn in thereafter.

Here, during the liquefied gas loading process (during bunkering), even if the liquefied gas storage tank 10 is cooled down, a lot of boil-off gas is generated when the liquefied gas is shipped. At this time, the internal pressure of the liquefied gas storage tank 10 may increase. There is a concern, a compressor is used to discharge the generated boil-off gas to the outside (Shore).

In addition, during the liquefied gas unloading process, in the warm-up stage, the compressor is used in the process of compressing the boil-off gas in order to increase the internal temperature of the liquefied gas storage tank 10 .

The H/D compressor 36 may implement both the compression process used during the liquefied gas loading process and the compression process used during the liquefied gas unloading process as described above.

That is, the H/D compressor 36 pressurizes the boil-off gas generated during bunkering and supplies it to shore, or warms up when unloading the liquefied gas (before maintenance of the liquefied gas storage tank 10). In the step, the BOG remaining in the liquefied gas storage tank 10 may be pressurized and returned to the liquefied gas storage tank 10 so that the BOG is circulated to the liquefied gas storage tank 10 .

Specifically, the H/D compressor 36 receives the boil-off gas generated from the liquefied gas storage tank 10 during bunkering through the seventh line L7, compresses it, and supplies it to the shore, When unloading the liquefied gas (in the case of maintenance of the liquefied gas storage tank 10), the boil-off gas remaining in the liquefied gas storage tank 10 is compressed and heated with a heater 361, and then the eighth line (L8) and Returning to the liquefied gas storage tank 10 through the 12th line (L12), BOG is liquefied gas storage tank 10, H/D compressor 36, heater 361, liquefied gas storage tank 10 It can be cycled sequentially. Accordingly, all of the liquefied gas stored in the liquefied gas storage tank 10 may be vaporized, and all of the vaporized liquefied gas may be discharged to the outside of the liquefied gas storage tank 10 .

In this case, the H/D compressor 36 may be a high duty compressor.

That is, the H/D compressor 36 is used to compress the boil-off gas generated during bunkering and discharge it to the shore, and at the same time, when unloading the liquefied gas (the liquefied gas storage tank 10 before maintenance starts). Case) may be used to pressurize the liquefied gas storage tank 10 to circulate by increasing the temperature of the remaining boil-off gas in order to vaporize all of the remaining liquefied gas stored in the liquefied gas storage tank 10 .

As described above, in the embodiment of the present invention, since the H/D compressor 36 can be used in common during bunkering, unloading of liquefied gas, or maintenance of the liquefied gas storage tank 10, the construction cost of the compressor is reduced and As a result, the space for system construction is reduced, which maximizes the space used in the ship.

The gas treatment system 1 according to the embodiment of the present invention is a technology for improving the reliquefaction rate by additionally providing a pressure reducing valve 341 together with the reliquefaction device 37, and a return pump according to the internal pressure of the gas-liquid separator 35 ( 35) and a technique for sharing a line through which BOG is supplied to the GCU 23 and the reliquefaction device 37 may be included.

The gas treatment system 1 according to the embodiment of the present invention includes a BOG compressor 30 for multi-stage pressurizing BOG generated in the liquefied gas storage tank 10, and BOG compressed in the BOG compressor 30. The reliquefaction device 37 for liquefying through the refrigerant, the first pressure reducing valve 341 for decompressing or expanding the BOG compressed in the BOG compressor 30, and the reliquefaction device for reducing or reducing at least a part of the BOG A second pressure reducing valve 342 that expands and a gas-liquid separator 35 that maintains the second reduced pressure of the reliquefied BOG through the second pressure reducing valve 342, and separates the gaseous and liquid phases as a main component do.

Here, the re-liquefaction device 37 may liquefy the boil-off gas branched from the middle end of the boil-off gas compressor 30 and compressed to a low pressure (13 bar to 15 bar) through a refrigerant, and more specifically, the boil-off gas compressor ( 30) branched from the middle stage and compressed to a low pressure (13 bar to 15 bar), the boil-off gas is first reduced to 7 bar to 8 bar through the first pressure reducing valve 341 and then cooled through the reliquefaction device 37, The cooled boil-off gas may be secondarily reduced in pressure to 5 bar to 6 bar through the second pressure reducing valve 342 .

As described above, in the embodiment of the present invention, a pressure reducing valve 342 is further provided at the rear end of the reliquefaction apparatus 37 to further improve the reliquefaction efficiency compared to the related art.

In addition, the gas-liquid separator 35 supplies the separated gas phase to the gas combustion device 23 that consumes flash gas through the heater 33 , and the separated liquid phase is transferred to the liquefied gas storage tank 10 . can return In the embodiment of the present invention, the return line (L10; 10th line) connecting the gas-liquid separator 35 and the liquefied gas storage tank 10, the bypass line L11 is bypassed on the return line L10; 11), a pump 38 (return pump) provided on the bypass line L11 to return the liquid liquefied gas stored in the gas-liquid separator 35 to the liquefied gas storage tank 10, and a first pressure reducing valve 341 ) and a branch line (not shown) branched between the reliquefaction device 37 and supplied to the gas combustion device 23 may be further included.

Specifically, when the internal pressure of the gas-liquid separator 35 is greater than or equal to the preset pressure value, the liquid gas stored in the gas-liquid separator 35 is returned to the liquefied gas storage tank 10 through the return line L10 (10th line). is supplied, and when the internal pressure of the gas-liquid separator 35 is less than the preset pressure value, the return pump 38 is driven to be supplied to the liquefied gas storage tank 10 through the bypass line L11 (11th line). have.

That is, since the gas-liquid separator 35 stores the BOG that has been secondarily decompressed to 5 bar to 6 bar through the second pressure reducing valve 342 , the liquid decompressed BOG is physically greater than the internal pressure of the liquefied gas storage tank 10 . Since it can be naturally supplied through the pressure gradient, which is a rule, when the internal pressure of the gas-liquid separator 35 is equal to or greater than the preset pressure value, the return pump 38 by supplying it to the liquefied gas storage tank 10 through the return line L10 There is an effect of preventing the consumption of driving power and implementing a stable return to the liquefied gas storage tank (10).

In addition, when the supply amount of the boil-off gas branched from the middle end of the boil-off gas compressor 30 and compressed to a low pressure is greater than the preset supply amount, the branch line is branched from the intermediate end of the boil-off gas compressor 30 and compressed to low pressure. When at least a portion of BOG is supplied to the gas combustion device 23, and the amount of BOG branched from the middle stage of the BOG compressor 30 and compressed to a low pressure is less than the preset supply amount, the BOG compressor 30 All of the boil-off gas branched from the middle end and compressed to a low pressure may be supplied to the reliquefaction apparatus 37 .

That is, the first pressure reducing valve 341 and the second pressure reducing valve 342 are provided together on the fourth line L4 to provide a side stream line of the BOG compressor 30 in addition to the fourth line L4. There is no need to do this, so the branching line of the BOG compressor 301 can be minimized, thereby improving the driving reliability of the system. (If the number of side stream lines of the BOG compressor 30 increases, the driving efficiency decreases. fell)

Here, the preset pressure value is 5 bar to 6 bar, the reliquefaction apparatus 37 uses a refrigerant as nitrogen, and the second pressure reducing valve 342 may be a Joule-Thomson valve.

The gas treatment system 1 according to the embodiment of the present invention reduces the delivery pressure of the boosting pump 40 when supplying the technology and liquefied gas to the high-pressure consumer 21 without a separate decompression to the low-pressure consumer 22 . It may include technology that can make it happen.

The gas processing system 1 according to the embodiment of the present invention is a boosting pump 40 for primary pressurizing the liquefied gas stored in the liquefied gas storage tank 10, and the liquefied gas first pressurized from the boosting pump 40 High-pressure pump 41 for receiving and secondary pressurization The vaporizer 42 for receiving and vaporizing the secondary pressurized liquefied gas from the high-pressure pump 41, the high-pressure liquefied gas or boil-off gas compressor 30 for vaporizing from the vaporizer 42 ), a high-pressure consumer 21 that receives and consumes pressurized BOG, a low-pressure consumer 22 that receives and consumes the BOG that is branched from the middle stage of the BOG compressor 30 and receives and consumes pressurized BOG, a liquefied gas storage tank It is provided between the forced vaporizer 50 and the forced vaporizer 50 and the low pressure demander 22 for receiving and forcibly vaporizing the liquefied gas stored in 10 and receiving the forced vaporized liquefied gas from the forced vaporizer 50 and A gas-liquid separator 51 for separating into a liquid phase is included as a main component.

The boosting pump 40 primarily pressurizes the liquefied gas stored in the liquefied gas storage tank 10 to supply it to the high-pressure pump 41 or the forced carburetor 50, through the boosting pump 40 to the high-pressure pump 41 ) and the use of the pump to supply the forced carburetor 50 can be shared.

Here, the forced vaporizer 50 receives the liquefied gas stored in the liquefied gas storage tank 10 in a first pressurized state from the boosting pump 40, vaporizes it, and then supplies it to the low-pressure consumer 22 to provide a low pressure without a separate decompression. Fuel can be supplied to the demand 22 . Through this, in the present embodiment, it is possible to omit the provision of a pressure reducing valve at the inlet end of the low pressure demander 22 .

In addition, the forced vaporizer 50 receives the liquefied gas stored in the liquefied gas storage tank 10 from the boosting pump 40 in a first pressurized state, vaporizes it, and then supplies it to the front end of the boil-off gas compressor 30 . can In this embodiment, since the required pressure of the consumer 20 is adjusted by the boil-off gas compressor 30 , there is an effect that the delivery pressure of the boosting pump 40 can be lowered. Of course, even in this case, the liquefied gas supplied to the forced vaporizer 50 may be supplied through the boosting pump 40 supplied with the liquefied gas to the high-pressure pump 41 .

As such, by sharing the use of the pump supplied to the high-pressure pump 41 and the forced carburetor 50 through the boosting pump 40, there is an effect that can reduce the construction cost of the pump 40, and the forced carburetor 50 ) by supplying the forcibly vaporized BOG to the front end of the BOG compressor 30, the liquefied gas delivery pressure from the liquefied gas storage tank 10 is lowered, thereby reducing the driving power of the pump 40.

In the gas treatment system 1 according to the embodiment of the present invention, the return line L10 of the gas-liquid separator 35 provided at the rear end of the reliquefaction apparatus 37 and the cool-down circulation line L13 of the high-pressure pump 42 are provided. , a technique of sharing at least one or more of each of the return lines (not shown) of the gas-liquid separator 51 provided at the rear end of the forced vaporizer 50 .

The gas treatment system 1 according to the embodiment of the present invention includes a reliquefaction device 37 for reliquefying the BOG compressed in the BOG compressor 30, and a vapor phase of the BOG reliquefied in the reliquefaction device 37. The gas-liquid separator 35 that separates the liquid from the liquid gas, the high-pressure pump 42 for pressurizing the liquefied gas stored in the liquefied gas storage tank 10, and the forced vaporizer 50 for forcibly vaporizing the liquefied gas is vaporized A gas-liquid separator 51 that separates and liquid phase, a cool-down circulation line (L13; line 13) connected from the high-pressure pump 42 to the liquefied gas storage tank 10 when the high-pressure pump 42 cools down, a gas-liquid separator The return line (L10; 10th line) of the gas-liquid separator 35 for returning the liquid phase of (35) to the liquefied gas storage tank 10 and the liquid phase of the gas-liquid separator 51 are returned to the liquefied gas storage tank 10 A return line (not shown) of the gas-liquid separator 51 is included as a main component.

In the embodiment of the present invention, when the high-pressure pump 41 cools down, the line L13 that returns from the high-pressure pump 41 to the liquefied gas storage tank 10, and the liquid phase of the gas-liquid separator 35 are transferred to the liquefied gas storage tank ( At least one line (L10) returning to 10) and a line returning the liquid phase of the gas-liquid separator (51) to the liquefied gas storage tank (10) may be shared.

As described above, at least one of the cool-down circulation line L13 of the high-pressure pump 41 , the return line L11 of the gas-liquid separator 35 , and the return line of the gas-liquid separator 51 is shared, thereby simplifying the structure of the return line. As a result, the driving reliability of the system is improved, the return can be stably implemented, and the return line is shared so that the cool-down can be performed in advance, so that the liquid boil-off gas recovers while returning to the liquefied gas storage tank (10). There is an effect that does not occur, that is, there is an effect that the actual re-liquefaction efficiency is increased.

For example, in the embodiment of the present invention, only the cool-down circulation line L13 of the high-pressure pump 41 and the return line of the gas-liquid separator 35 may be shared.

When the high-pressure consumer 21 is driven through the liquefied gas and the boil-off gas is re-liquefied by the re-liquefaction device 37 at the same time, the discharge pressure of the gas-liquid separator 35, that is, the return line L10 The pressure is about 5-6 bar, and the cool-down circulation line L13 of the high-pressure pump 41 corresponds to about 9 bar, so in the case of the return line L10, a back pressure is applied to the gas-liquid separator 35, and a problem may occur.

However, in the embodiment of the present invention, since the case where the high-pressure consumer 21 is driven through the liquefied gas and the case where the BOG is re-liquefied by the re-liquefaction device 37 does not occur at the same time, the high-pressure pump ( By sharing only the cool-down circulation line L13 of 41 and the return line of the gas-liquid separator 35, it is possible to prevent back pressure from being applied on the shared line and effectively share the return line. (The reliquefaction device 37 is driven This is a case where BOG remains. In this case, since a sufficient amount of BOG is supplied to the high-pressure consumer 21 through the BOG compressor 30, the liquefied gas is transferred to the high-pressure consumer through the high-pressure pump 41 ( There is no need to send it to 21), so there is no case where the high-pressure pump 41 is driven.)

As another example, in the embodiment of the present invention, the cool-down circulation line L13 of the high-pressure pump 41 and the return line of the gas-liquid separator 51 are shared only when both the high-pressure demander 21 and the low-pressure demander 22 are driven. can be

The forced carburetor 50 operates only when the low-pressure demander 22 is driven, and the high-pressure pump 41 operates only when the high-pressure demander 21 is driven, so that the high-pressure and low-pressure demanders 21 and 22 are Only when all are operated, the cool-down circulation line L13 of the high-pressure pump 41 and the return line of the gas-liquid separator 51 can be shared.

For this reason, the return line of the gas-liquid separator 51 is pre-cooled by the cool-down of the high-pressure pump 41 , so that the liquid returned from the gas-liquid separator 51 to the liquefied gas storage tank 10 is not regasified, so that the liquefied gas storage tank The internal pressure of (10) can be efficiently managed. Of course, at this time, the return line of the gas-liquid separator 51 and the cool-down circulation line L13 of the high-pressure pump 41 flow at different times, so that the problem of back pressure does not occur. (The cool-down of the high-pressure pump 41 is It is driven only at the beginning of supply to the high-pressure consumer 21, and the return line of the gas-liquid separator 51 is continuously driven while being supplied to the low-pressure demand 22).

The gas treatment system 1 according to the embodiment of the present invention connects the front end of the forced vaporizer 50 with the return line of the gas-liquid separator 51 to simplify the cool-down of the return line of the gas-liquid separator 51. may include

The gas treatment system 1 according to the embodiment of the present invention includes a gas-liquid separator 51, a gas-liquid separator 51 that separates the forcibly vaporized liquefied gas into a gas phase and a liquid phase from the forced vaporizer 50 for forcibly vaporizing the liquefied gas. A return line of the gas-liquid separator 51 for returning the liquid phase of the liquid gas to the liquefied gas storage tank 10, and a bypass line connecting the front end of the forced vaporizer 50 and the return line of the gas-liquid separator 51 (not shown) is included as the main component.

In the embodiment of the present invention, a bypass line connecting the front end of the forced vaporizer 50 and the return line of the gas-liquid separator 51 is provided, and the bypass line of the forced vaporizer 50 and the return of the gas-liquid separator 51 are provided. You can share lines together.

Through this, the bypass line of the forced vaporizer 50 is connected to the return line of the gas-liquid separator 51 rather than the front end of the gas-liquid separator 51, and the bypass function of the forced vaporizer 50 and the return line of the gas-liquid separator 51 are connected. Since the cool-down function can be shared, there is an effect that the cool-down of the gas-liquid separator 51 is simplified and optimized.

The gas treatment system 1 according to the embodiment of the present invention may include a technology of supplying engine coolant and steam in parallel and in series to supply a heat source to the glycol water used in the carburetor 42 .

Hereinafter, it will be described with reference to FIGS. 2A to 2C. However, first and second embodiments of the vaporizer (42a, 42b) will be described together.

2A and 2B are conceptual diagrams of a vaporization system in the gas processing system of the present invention.

The vaporizer 1 and the second embodiment (42a, 42b) of the gas treatment system (1) according to the embodiment of the present invention, the vaporizer 424 for vaporizing the liquefied gas stored in the liquefied gas storage tank 10 through the vaporization fruit ; vaporization heat exchanger), a first heat exchanger 4231 for exchanging heat between the vaporized fruits and engine coolant, a second heat exchanger 4232 for supplying a heat source to the vaporized fruits (second supplying unit for vaporized fruits) and vaporization It includes a circulation pump 422 that circulates the heat medium to supply the vaporizer 424 .

Specifically, in the vaporizer first and second embodiments 42a and 42b of the gas processing system 1 according to the embodiment of the present invention, the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232 ) may supply a heat source to the vaporized fruit in the order of the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232, more specifically, the circulation pump 422, the vaporized fruit first supply device ( 4231), the vaporized fruit second supply device 4232 may be serially connected in the order, or the vaporized fruit first supply device 4231, the circulation pump 422, and the vaporized fruit second supply device 4232 may be connected in series in this order.

Here, as for the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232, the vaporized fruit first supply device 4231 is a plate method, and the vaporized fruit second supply device 4232 is a Shell & Tube method. provided so that the types of heat exchangers may be different from each other. Of course, the two heat exchangers may be used in the same type as a plate method or a shell & tube method. In addition, the vaporized fruit second supply device 4232 may use steam or seawater as a heat source supplied to the vaporized fruit.

In the first and second embodiments 42a and 42b of the vaporizer of the gas treatment system 1 according to the embodiment of the present invention, the first supply of vaporized fruits by connecting the front end and the rear end of the vaporized fruit first supply device 4231 A first bypass line (GBL1; vaporized fruit first branch line) that bypasses the vaporized fruit passing through the device 4231 from the rear end to the front end of the vaporized fruit first supply device 4231, the second vaporized fruit supply device 4232 ) by connecting the front end and the rear end of the second bypass line (GBL2; vaporized fruit product) that bypasses the vaporized fruit passing through the vaporized fruit second supply device 4232 from the rear end of the second vaporized fruit supply device 4232 to the front end 2 branch line) and a control unit 902 for controlling the first bypass line GBL1 or the second bypass line GBL2 and a vaporized fruit storage tank 421 for storing vaporized fruits may be further included.

When the vaporized fruit supplied to the vaporizer 424 is below the preset temperature value, the control unit 902 drives the vaporized fruit first branch line (GBL1) or the vaporized fruit second branch line (GBL2) to reheat the vaporized fruit can Here, the preset temperature value is 85 degrees to 95 degrees zero, and the second vaporized fruit supply device 4232 may be supplied with a heat source depending on the heat source supply capability of the vaporized fruit first supply device 4231 .

When describing the process of heating/cooling circulation of the vaporized fruits in the first embodiment 42a of the vaporizer of the gas treatment system according to an embodiment of the present invention, the vaporized fruits stored in the vaporized fruit storage tank 421 are vaporized fruits circulating It is circulated through the pump 422 and heated through the engine coolant (jacket cooling water) by the first vaporized fruit supply device 4231 to be heated up to a maximum of 70 degrees, and then the vaporized fruit second supply device 4232 It can be supplied to and heated through steam or seawater to be heated to about 85 to 95 degrees (preferably 90 degrees), and then supplied to the vaporization heat exchanger 424 to flow through the first line L1. The liquefied gas at 130 degrees can be heated to 35 to 55 degrees, and the vaporized refrigerant can be cooled from 90 degrees to 50 degrees.

Here, the engine cooling water is supplied by the vaporized fruit first supply device 4231 and when heated, the amount of engine coolant varies depending on the driving of the engine, so the heat source supply amount of the engine cooling water can be reduced when the engine is driven at a low speed. (4232) is variable depending on the vaporized fruit first supply device (4231) can be operated by heating. This may be implemented by the driving of the above-described control unit 902, the control unit 902, the temperature information of the liquefied gas or vaporized fruit from the first temperature measuring device 921 and the second temperature measuring device 922 It may be transmitted by wire or wirelessly, and based on this, the vaporized fruit may be heated by driving the first bypass line GBL1 or the second bypass line GBL2 according to the above-described situation.

In the second embodiment 42b of the vaporizer of the gas treatment system 1 according to the embodiment of the present invention, the heating/cooling cycle of the vaporized fruits will be described. The vaporized fruits first supply device 4231 and the vaporized fruits circulation pump Since only the order of (422) has been changed, other than that, it is the same as described in the above-described first embodiment of the vaporizer (42a), so it will be replaced therewith.

Hereinafter, the vaporizer will be described with respect to the third embodiment (42c).

2C is a conceptual diagram of a vaporization system in the gas processing system of the present invention.

The vaporizer third embodiment 42c of the gas treatment system 1 according to the embodiment of the present invention includes a vaporization heat exchanger 424, a vaporized fruit first supply device 4231, a vaporized fruit second supply device 4232, Circulation pump 422, a heater 4233 provided at the rear end of the vaporized fruit first supply device 4231 and additionally heats the vaporized fruit heated in the vaporized fruit first supply device 4231 (additional vaporized fruit heater) and vaporized fruit A bypass line (GBL4; vaporized fruit) provided at the rear end of the first supplying device 4231 and supplying the vaporized fruit heated by the vaporized fruit first supplying device 4231 to the front end of the second vaporized fruit supplying device 4232 3rd branch line).

The vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232 are, the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232 are connected in parallel, and the vaporized fruit first The supply device 4231 heats the vaporized fruit first, the second vaporized fruit supply device 4232 can heat the vaporized fruit suboptimally, and the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232 ), may be disposed at the rear end of the circulation pump 422 .

Specifically, the vaporized fruit heated by the vaporized fruit first supply device 4231 is heated to the vaporized fruit through the heater 4233 when the temperature of the rear end of the vaporized fruit first supply device 4231 is less than or equal to the preset temperature. Alternatively, the vaporized fruit may be supplied to the front end of the second supply device 4232 through the bypass line GBL4.

Here, the vaporized fruit first supply device 4231 is a plate method, and the vaporized fruit second supply device 4232 is a Shell & Tube method, and the two heat exchangers may be different in type, and of course, the two heat exchangers are a Plate method or a Shell & Tube method. may be used in the same type. The vaporized fruit second supply device 4232 may use steam or seawater as a heat source supplied to the vaporized fruit.

When describing the process in which the vaporized fruit is heated/cooled in the vaporizer third embodiment 42c of the gas treatment system 1 according to the embodiment of the present invention, the vaporized fruit stored in the vaporized fruit storage tank 421 is vaporized It is circulated through the heat medium circulation pump 422 and is heated through the engine cooling water (jacket cooling water) by the vaporized fruit first supply device 4231 to be heated up to a maximum of 90 degrees.

However, since the amount of engine coolant varies according to the driving of the engine, it may be difficult to always supply a constant heat source to the vaporization heat exchanger 424 due to severe temperature change. In order to prevent this, the present invention may further include a vaporized fruit additional heater (4233). In the present invention, when the engine is driven at a low speed and the heat source supply amount of the engine coolant is reduced, it can be heated up to 90 degrees by reheating through the vaporized fruit additional heater 4233 . Thereafter, the liquefied gas of -130 degrees below zero which is supplied to the vaporization heat exchanger 424 and flows through the first line L1 can be heated to 35 to 55 degrees, and the vaporized refrigerant can be cooled from 90 degrees to 50 degrees. .

Here, the vaporized fruit second supply device 4232 may be variable and operated by heating depending on the vaporized fruit first supply device 4231 . This may be implemented by the driving of the above-described control unit 902, the control unit 902, the temperature information of the liquefied gas or vaporized fruit from the first temperature measuring device 921 and the second temperature measuring device 922 It may be transmitted by wire or wirelessly, and based on this, the vaporized fruit may be heated by driving the first bypass line GBL1 or the second bypass line GBL2 according to the above-described situation.

In addition, the second vaporized fruit supply device 4232, the engine is stopped for a long period of time, so that the supply of engine cooling water is very small. When the heating amount is insufficient even with the vaporized fruit additional heater 4233, the vaporized fruit is the third vaporized fruit Since it is not supplied to the branch line GBL3 but to the vaporized fruit circulation line GL, the vaporized fruit can be heated up to 90 degrees above zero.

In the third embodiment 42c of the carburetor according to an embodiment of the present invention, since the amount of engine coolant varies depending on the driving of the engine, when the heat source supply amount of the engine coolant is reduced when the engine is driven at a low speed, the fourth branch line GBL4 ) can be bypassed to the second vaporized fruit supply device 4232 through ) and heated to an image of 90 degrees by the vaporized fruit second supply device 4232

As described above, through the parallel or series connection of the vaporized fruit supply device described above, the flow rate of steam is reduced due to the engine coolant through the heating technology of the vaporized fruit, thereby reducing the boiler operation, so fuel consumption can be reduced, and the series or parallel connection Therefore, there is an effect that the driving reliability of the vaporizer 42 is improved.

The gas processing system 1 according to the embodiment of the present invention may include a technology for implementing the processing of liquefied gas and boil-off gas through parallel driving according to the internal pressure of the liquefied gas storage tank 10 .

The gas processing system 1 according to the embodiment of the present invention is a liquefied gas processing device for supplying to a consumer by pressurizing/heating the liquefied gas stored in the boil-off gas compressor 30 and the liquefied gas storage tank 10 provided in parallel. (40, 41, 42), a re-liquefaction device 37 for re-liquefying the BOG compressed by the BOG compressor 30, is provided at the rear end of the re-liquefaction device 37 and is liquefied by the re-liquefaction device 37 A second pressure reducing valve 342 for decompressing or expanding the boil-off gas, a gas combustion device 23 for consuming the boil-off gas, and a forced vaporizer 50 for forcibly vaporizing the liquefied gas stored in the liquefied gas storage tank 10 are the main components. included in the composition.

Here, the liquefied gas processing devices 40 , 41 , 42 receive the pressurized liquefied gas supplied from the boosting pump 40 , the boosting pump 40 for primary pressurizing the liquefied gas stored in the liquefied gas storage tank 10 . and a high-pressure pump 41 for secondary pressurization and a vaporizer 42 for receiving and vaporizing the liquefied gas pressurized at high pressure from the high-pressure pump 41, and the boil-off gas compressor 30 is provided in parallel to provide the first boil-off gas It may be provided as a compressor (not shown) and a second boil-off gas compressor (not shown).

Hereinafter, the first parallel operation of the gas treatment system 1 according to the internal pressure of the liquefied gas storage tank 10 will be described.

The first preset pressure is the internal pressure of the liquefied gas storage tank 10 when the amount of BOG in the liquefied gas storage tank 10 is 75 to 85%, and the second preset pressure is the first preset pressure Greater than and less than 1,12 bar, the third preset pressure is smaller than the first preset pressure and greater than 1.06 bar, and the fourth preset pressure is smaller than the third preset pressure and greater than 1.03 bar.

First, the first boil-off gas compressor is basically driven. When the internal pressure of the liquefied gas storage tank 10 is equal to or greater than the first preset pressure, the second boil-off gas compressor is additionally driven, and when the internal pressure of the liquefied gas storage tank 10 is less than the first preset pressure, the liquefied gas processing device (40,41,42) is driven further.

BOG generated in the liquefied gas storage tank 10 may be supplied to the re-liquefaction device 37 or the gas combustion device 23 when the internal pressure of the liquefied gas storage tank 10 is equal to or greater than the second preset pressure. , when the internal pressure of the liquefied gas storage tank 10 is equal to or greater than the second preset pressure, and the fuel requirement of the consumer 20 is greater than or equal to the preset requirement, the liquefied gas processing devices 40, 41, and 42 may be additionally driven have.

In addition, when the internal pressure of the liquefied gas storage tank 10 is less than the third preset pressure, the driving of the first boil-off gas compressor can be stopped, and when the internal pressure of the liquefied gas storage tank 10 is less than the fourth preset pressure , by forcibly vaporizing the liquefied gas stored in the liquefied gas storage tank 10 through the forced vaporizer 50 , and returning the forcibly vaporized liquefied gas back to the liquefied gas storage tank 10 , the internal pressure of the liquefied gas storage tank 10 . can elevate

At this time, in the embodiment of the present invention, a control unit (not shown) and a pressure measuring device (not shown) for measuring the internal pressure of the liquefied gas storage tank 10 and a fuel requirement measuring device for measuring the fuel requirement of the demander 20 ( not shown), and the control unit receives information from the pressure measuring device and the fuel requirement measuring device by wire or wirelessly so that the internal pressure of the above-described liquefied gas storage tank 10 is determined by the first to fourth groups. It is possible to control the liquefied gas processing devices 40 , 41 , 42 and the boil-off gas compressor 30 for fluctuations according to the set pressure.

As described above, in the embodiment of the present invention, the BOG compressor 30 and the liquefied gas processing devices 40, 41, 42 are driven in parallel so that the demand 20 can be flexibly driven without oil supply, There is an effect of reducing the system construction cost.

The gas processing system 1 according to the embodiment of the present invention implements the processing of liquefied gas, boil-off gas, and oil through parallel driving according to the flow of the internal pressure when the internal pressure of the liquefied gas storage tank 10 is low. may include technology.

The gas processing system 1 according to the embodiment of the present invention includes a boil-off gas compressor 30 , a reliquefaction device 37 , liquefied gas processing devices 40 , 41 , 42 , a second pressure reducing valve 342 , and an oil An oil treatment device (not shown) for supplying the oil stored in the storage tank (not shown) to the customer 20 is included as a main component.

Hereinafter, the second parallel operation of the gas treatment system 1 according to the internal pressure of the liquefied gas storage tank 10 will be described.

The BOG compressor 30 is basically driven at a first preset pressure, and when the amount of BOG generated in the liquefied gas storage tank 10 is greater than the fuel required amount of the demander 20, the reliquefaction device 37 is installed. When additional operation is performed and the amount of boil-off gas generated in the liquefied gas storage tank 10 is less than the fuel required amount of the consumer 20, the liquefied gas processing devices 40, 41, 42 and the oil processing device may be additionally operated. . Preferably, the liquefied gas processing devices 40 , 41 , and 42 may be operated first, and the oil processing device may be operated secondarily.

Here, the first preset pressure may be an internal pressure of the liquefied gas storage tank 10 when the amount of BOG in the liquefied gas storage tank 10 is 75 to 85%, or 1.06 bar to 1.12 bar.

At this time, in the embodiment of the present invention, the control unit receives information from the pressure measuring device and the fuel requirement measuring device by wire or wirelessly so that the internal pressure of the above-described liquefied gas storage tank 10 is changed according to the first preset pressure. The liquefied gas processing apparatus 40 , 41 , 42 , the boil-off gas compressor 30 and the oil processing apparatus may be controlled.

As described above, in the embodiment of the present invention, the BOG compressor 30, the liquefied gas processing devices 40, 41, 42, and the oil processing device are driven in parallel to satisfy the homeostasis of the fuel supply of the system, thereby driving reliability of the system. This has an improved effect.

The gas processing system 1 according to the embodiment of the present invention implements the processing of liquefied gas, boil-off gas, and oil through parallel operation according to the flow of the internal pressure when the internal pressure of the liquefied gas storage tank 10 is high. may include technology.

The gas processing system 1 according to the embodiment of the present invention includes the boil-off gas compressor 30 and the reliquefaction device 37 provided in parallel as main components. Here, the boil-off gas compressor 30 may be provided in parallel to be provided as a first boil-off gas compressor (not shown) and a second boil-off gas compressor (not shown).

Hereinafter, the control operation of the gas treatment system 1 according to the internal pressure of the liquefied gas storage tank 10 will be described.

When the internal pressure of the liquefied gas storage tank 10 is equal to or greater than the preset pressure, the first boil-off gas compressor is operated to supply it to the consumer 20, and the amount of fuel generated in the liquefied gas storage tank 10 is higher than the fuel required by the consumer 20 When the amount of BOG is larger, the reliquefaction device 37 may be additionally operated or the second BOG compressor may be additionally operated. Preferably. By first operating the second boil-off gas compressor and supplying it to the consumer 20, the ship's speed can be increased, and the reliquefaction device 37 can be operated in the next lane. In this case, the preset pressure may be 1.11 bar to 1.13 bar.

As described above, in the embodiment of the present invention, the BOG compressor 30 is driven in parallel and the reliquefaction device 37 is further driven to efficiently process the BOG continuously discharged from the liquefied gas storage tank 10 to store the liquefied gas. There is an effect that can stabilize the internal pressure of the tank (10).

Although the present invention has been described in detail through specific examples, this is for the purpose of describing the present invention in detail, and the present invention is not limited thereto, and by those of ordinary skill in the art within the technical spirit of the present invention. It will be clear that the transformation or improvement is possible.

All simple modifications and variations of the present invention fall within the scope of the present invention, and the specific scope of protection of the present invention will be made clear by the appended claims.

1: gas treatment system 10: liquefied gas storage tank
20: consumer 21: high voltage demand
22: Low pressure demand 23: Gas combustion unit (GCU)
24: vent mast 25: safety valve
30: boil-off gas compressor 33: heater
341: first pressure reducing valve 342: second pressure reducing valve
35: gas-liquid separator 36: H/D compressor
361: heater 37: reliquefaction device
38: return pump 40: boosting pump
41: high pressure pump 42: carburetor
421: vaporized fruit storage tank 422: vaporized fruit circulation pump
423: vaporized fruit supply device 4231: vaporized fruit first supply device
4232: vaporized fruit second supply device 4233: vaporized fruit additional heater
424: vaporization heat exchanger 50: forced vaporizer
51: gas-liquid separator 52: heater
902: control unit 921: first temperature measuring device
922: second temperature measuring device
L1 to L13: first to thirteenth lines GL: vaporized fruit circulation line
GLb: Vaporized fruit branch line GBL1: Vaporized fruit first branch line
GBL2: Vaporized fruit 2nd branch line GBL3: Vaporized fruit 3rd branch line
GBL4: Vaporized fruit 4th branch line

Claims (10)

a vaporizer for vaporizing the liquefied gas stored in the liquefied gas storage tank through vaporization fruit;
a first heat exchanger for exchanging heat between the vaporized fruit and engine coolant; and
A second heat exchanger for supplying a heat source to the vaporized fruit,
The first heat exchanger and the second heat exchanger,
supplying a heat source to the vaporized fruit in the order of the first heat exchanger and the second heat exchanger,
a first bypass line connecting the front end and the rear end of the first heat exchanger to bypass the vaporized fruit passing through the first heat exchanger from the rear end to the front end of the first heat exchanger;
a second bypass line connecting the front end and the rear end of the second heat exchanger to bypass the vaporized fruit passing through the second heat exchanger from the rear end to the front end of the second heat exchanger; and
Gas processing system, characterized in that it further comprises a control unit for controlling the first bypass line or the second bypass line The method of claim 1,
Further comprising a circulation pump circulating to supply the vaporized fruit to the vaporizer,
The first heat exchanger and the second heat exchanger are
The circulation pump, the first heat exchanger, and the second heat exchanger are connected in series in this order. The method of claim 1,
Further comprising a circulation pump circulating to supply the vaporized fruit to the vaporizer,
The first heat exchanger and the second heat exchanger are
The first heat exchanger, the circulation pump, and the second heat exchanger are connected in series in this order. According to claim 1, wherein the first heat exchanger and the second heat exchanger,
A gas treatment system, characterized in that the types of heat exchangers are different. 5. The method of claim 4, wherein the first heat exchanger and the second heat exchanger,
A gas treatment system, characterized in that the type of heat exchanger is the same. According to claim 1, wherein the second heat exchanger,
A gas treatment system, characterized in that steam or seawater is used as a heat source supplied to the vaporized fruit. delete According to claim 1, wherein the control unit,
When the vaporized fruit supplied to the vaporizer is below a preset temperature value, the first bypass line or the second bypass line is driven to reheat the vaporized fruit. The method of claim 8, wherein the preset temperature value is
A gas processing system, characterized in that the image is 85 degrees to the image 95 degrees. According to claim 1, wherein the second heat exchanger,
The gas treatment system, characterized in that the heat source is supplied depending on the heat source supply capability of the first heat exchanger.

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