KR102162157B1 - Treatment system of gas - Google Patents

Abstract

A gas processing system according to an embodiment of the present invention includes a vaporizer for vaporizing liquefied gas stored in a liquefied gas storage tank through a vaporized fruit; A first heat exchanger for exchanging the vaporized fruit and engine coolant; And a second heat exchanger supplying a heat source to the vaporized fruit, wherein the first heat exchanger and the second heat exchanger are connected in parallel with the first heat exchanger and the second heat exchanger, and the first heat exchanger provides the vaporized fruit. It is characterized in that the heating is performed first, and the second heat exchanger heats the vaporized fruit sub-optimally.

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 navigates the ocean with a large amount of minerals, crude oil, natural gas, or more than a few thousand containers. It is made of steel, and the thrust generated by the rotation of the propeller while floating on the water surface by buoyancy Go through.

Such ships generate thrust by driving the 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 rotates and the propeller is driven. It was common to be able to.

However, in recent years, LNG carriers carrying liquefied natural gas use LNG as fuel to drive the engine, and the LNG fuel supply method is used. It is also applied to other ships.

In general, it is known that LNG is a clean fuel and its reserves are also richer than petroleum, and its usage is rapidly increasing as mining and transportation technologies are developed. Such LNG is generally stored in a liquid state by lowering the temperature of methane, which is the main component, to -162 degrees or less under 1 atmosphere, and the volume of liquefied methane is about one-600th of the volume of methane in the gaseous state, which is the standard state, and the specific gravity Silver is 0.42, which is about one-half of the specific gravity of crude oil.

However, the temperature and pressure required to drive the customer 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 that controls the temperature and pressure of LNG stored in a liquid state and supplies it to a customer.

In addition, when LNG is stored in a liquid state, some LNG is vaporized as heat permeation occurs into the tank to generate boil off gas (BOG).In the past, boil off gas (BOG) is generated by lowering the tank pressure to remove the risk of damage to the tank. It was simply discharged to the outside. However, in recent years, the necessity of development is gradually increasing for a utilization plan such as re-liquefying the boil-off gas generated in the tank and supplying it to a customer.

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 that effectively supplies liquefied gas and/or boil-off gas from a liquefied gas storage tank to a customer.

The gas treatment system according to the present invention comprises: a vaporizer for vaporizing liquefied gas stored in a liquefied gas storage tank through a vaporized fruit; A first heat exchanger for exchanging the vaporized fruit and engine coolant; And a second heat exchanger supplying a heat source to the vaporized fruit, wherein the first heat exchanger and the second heat exchanger are connected in parallel with the first heat exchanger and the second heat exchanger, and the first heat exchanger provides the vaporized fruit. It is characterized in that the heating is performed first, and the second heat exchanger heats the vaporized fruit sub-optimally.

Specifically, the first heat exchanger further includes a heater provided at a rear end of the first heat exchanger to further heat the vaporized fruit heated in the first heat exchanger, and the vaporized fruit heated by the first heat exchanger comprises: the first heat exchanger When the temperature at the rear end of the group is less than or equal to a preset temperature, the vaporized fruit may be heated through the heater.

Specifically, a bypass line provided at a rear end of the first heat exchanger and configured to supply the vaporized heat heated in the first heat exchanger to a front end of the second heat exchanger, further comprising: The heated vaporized fruit may be supplied to the front end of the second heat exchanger through the bypass line when the temperature at the rear end of the first heat exchanger is less than or equal to a preset temperature.

Specifically, a circulation pump circulating to supply the vaporized fruit to the vaporizer may be further included, and the first heat exchanger and the second heat exchanger may be disposed at a rear end of the circulation pump.

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 vaporization nutrient.

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 customer.

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

Objects, specific advantages and novel features of the present invention will become more apparent from the following detailed description and preferred embodiments associated with the accompanying drawings. In adding reference numerals to elements of each drawing in the present specification, it should be noted that, even though they are indicated on different drawings, only the same elements are to have the same number as possible. In addition, in describing the present invention, when it is determined that a detailed description of related known technologies 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 refer to LNG (Liquefied Natural Gas), and the boil-off gas may refer to BOG (Boil Off Gas), such as naturally vaporized LNG.

Liquefied gas may be referred to regardless of state change, such as a liquid state, a gas state, a liquid and gas mixture state, a supercooled state, and a supercritical state, and it is noted that the boil-off gas is the same. In addition, the present invention is not limited to liquefied gas to be treated, and may be a liquefied gas treatment system and/or a boil-off gas treatment system.

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

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

Hereinafter, each configuration of the gas treatment system 1 according to an embodiment of the present invention will be described, and after the description of the configuration is completed, each embodiment will be described through the 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 adjustment 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, or a pressurized type, and the size, shape, structure, etc. are not particularly limited as long as the liquefied gas can be stored.

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

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, it is preferable to discharge the liquefied gas storage tank 10 for protection. Accordingly, the present invention can properly discharge the boil-off gas according to the pressure of the liquefied gas storage tank 10.

The discharged boil-off gas 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 boil-off gas discharged from the liquefied gas storage tank 10 is cooled to a boiling point or lower by a re-liquefaction device 37, which will be described later, to be liquefied from a gaseous state to a liquid state (same as the liquefied gas as a liquefied vaporized gas/ Similar) It can be treated such as returning to the liquefied gas storage tank (10).

The liquefied gas storage tank 10 may include an insulation portion and a barrier portion to prevent penetration of external heat.

The barrier portion may be provided on the inner side (a side adjacent to the liquefied gas) compared to the heat insulation portion, and the insulation portion may be provided on the outside (a side adjacent to the hull) compared 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, or a pressurized type.

The heat insulation part insulates the inside and outside of the liquefied gas storage tank 10 using a heat insulation 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 be provided with metal such as stainless steel (SUS) and INVAR.

When the liquefied gas storage tank 10 is of a membrane type, the structure of the insulation may be determined according to a conventionally well-known type such as Mark III and No. 96, and when the liquefied gas storage tank 10 is a stand-alone type, MOSS, SPB, etc. The structure may be determined according to a conventionally known type of. Of course, the structure of the heat insulating part 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 insulation part, and/or between the outer wall and the heat insulation part of the liquefied gas storage tank 10 .

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

The consumer 20 is a configuration that consumes liquefied gas (liquefied gas, evaporative gas, flash gas) and the like, and may be configured to generate or burn energy while consuming liquefied gas or the like.

As an example, the customer 20 is a low pressure customer using a 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 reliquefaction device, a boiler, and a gas combustion device. A high-pressure engine (ME-GI engine, etc.) may be a high-pressure consumer using a liquefied gas having a pressure of about 200 bar to 400 bar (absolute pressure), and the like, and the pressure of the liquefied gas required for each consumer 20 may be different.

That is, in the present invention, the consumer 20 comprehensively 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 an embodiment of the present invention, a gas supply unit for processing liquefied gas or boil-off gas stored in the liquefied gas storage tank 10 is provided. Here, the gas supply unit is a configuration for delivering liquefied gas and/or boil-off gas to a customer 20 such as an engine, and the boil-off gas compressor 30, boosting pump 40, high pressure pump 41, carburetor 42, etc. Can include.

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

In this case, the plurality of boil-off gas compressors 30 constituting the boil-off gas compression unit may be provided so that all of the centrifugal type, all of the reciprocating type, or the centrifugal type and the reciprocating type are mixed.

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

For example, in the present invention, the boil-off gas compressor 30 may be configured as a centrifugal type, such as 2 stages, 3 stages, 5 stages, 6 stages, and the like. Each of the stages is compressed only according to the requirements of the boil-off gas to be supplied according to the type of the customer 20, but the larger the number of stages does not indicate that the discharge pressure is relatively large.

In addition, the boil-off gas compressor 30 may be configured as a cryogenic compressor to process boil-off gas at a low temperature of about -100° C. discharged from the liquefied gas storage tank 10. However, when the boil-off gas is compressed by the boil-off gas compressor 30, the temperature of the boil-off gas may increase, so some of the upstream boil-off gas compressors among the multi-stage boil-off gas compressors included in the boil-off gas compression unit are cryogenic compressors. , The remaining boil-off gas compressors downstream may be room temperature compressors.

When the temperature of the boil-off gas is increased 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. This can cause an unnecessary increase in the load of the boil-off gas compressor 30, and at least one boil-off gas compressor 30 upstream and/or downstream of at least one boil-off gas compressor 30, compressed evaporation An evaporative gas cooler (not shown) for cooling the gas may be provided.

The boil-off gas cooler can cool the boil-off gas using a variety of cold heat sources. For example, the boil-off gas cooler includes seawater, re-liquefied refrigerant of the re-liquefaction device 37, liquefied gas, boil-off gas, flash gas, etc. Can be used.

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

The boil-off gas flowing into the boil-off gas compressor 30 may be heat-exchanged with the compressed boil-off gas. However, the boil-off gas flowing into the boil-off gas compressor 30 due to heat exchange may be preheated, and thus, the boil-off gas compressor 30 may be configured as a room temperature compressor.

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

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

That is, in the boil-off gas compression unit having the boil-off gas compressor 30 provided in multiple stages, the pressure of boil-off gas supplied to each customer 20, the number of boil-off gas compressors 30, the degree of multi-stage compression of boil-off gas, etc. It is not limited and can be determined in various ways.

In order to deliver the boil-off gas from the liquefied gas storage tank 10 to the low-pressure consumer 22 or the high-pressure consumer 21 through the boil-off gas compressor 30, supply from the liquefied gas storage tank 10 to each consumer 20 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 boil-off gas compressor (end or intermediate stage, etc.) to the low-pressure consumer 22 may be a low-pressure supply line (third line (L3)), and the boil-off gas compressor 30 (end or intermediate stage, etc.) The supply line connected to the high-pressure consumer 21 may be a high-pressure supply line (second line L2). Accordingly, the supply line may be divided into a low pressure supply line (third line (L3)) and a high pressure supply line (second line (L2)) based on the boil-off gas compressor 30.

The boil-off gas compressor 30, when passing through only a part of the boil-off gas compressors 30 provided in multiple stages, is compressed to a low pressure and supplied to the low-pressure consumer 22 along the low-pressure supply line L3, and is provided in multiple stages. After passing through all of the boil-off gas compressors 30, the boil-off gas can be compressed to a high pressure and supplied to the high-pressure consumer 21 along the high-pressure supply line L2.

In the boil-off gas compressor 30, some may not use lubricating oil, and the rest may use lubricating oil. For example, if the boil-off gas compressor 30 is provided in five stages, the boil-off gas compressors of the first to third stages do not use lubricating oil (lubricating oil is not mixed with the boil-off gas), and the fourth to fifth stages use lubricating oil. Can (lubricating oil is mixed into the boil-off gas). This is because, in the case of the high-pressure stage, as the pressure of the boil-off gas changes to high pressure, the lubricating oil is required in order to smoothly drive the piston of the boil-off gas compressor 30.

Of course, the number of boil-off gas compressors 30 is not limited to the above, and a part of the front end (low-pressure end) of the plurality of boil-off gas 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 depressurize or expand a boil-off gas to be pressurized by the boil-off gas compressor 30 and supplied to the reliquefaction device 37. Although not shown here, the first pressure reducing valve 341 depressurizes or expands the boil-off gas pressurized by the boil-off gas compressor 30 and can be supplied to the reliquefaction device 37 as well as the gas combustion device 23. .

The first pressure reducing valve 341 may be provided together with the second pressure reducing valve 342 to reduce or expand a multistage boil-off gas pressurized by the boil-off gas compressor 30. For example, the first pressure reducing valve 341 may first depressurize or first expand the boil-off gas pressurized by the boil-off gas compressor 30 or the boil-off gas branched and supplied to the intermediate end of the boil-off gas compressor 30, The boil-off gas supplied to the liquefaction device 37 and heat-exchanged in the reliquefaction device 37 may be re-liquefied by secondary pressure reduction or secondary expansion through the second pressure reducing valve 342 again.

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

The gas-liquid separator 35 separates gas from the boil-off gas depressurized or expanded by the first pressure reducing valve 341 or the second pressure reducing valve 342. In the gas-liquid separator 35, the boil-off gas is separated into liquid and gas, so that 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 depressurized by the first pressure reducing valve 341 or the second pressure reducing valve 342 and cooled. 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 about 45 degrees. The boil-off gas that has risen to a temperature of around 45 degrees is recovered to the reliquefaction device 37 through the first pressure reducing valve 341, and the boil-off gas heat-exchanged in the reliquefaction device 37 is returned to the second pressure reducing valve 342. Is supplied as 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 reduced in pressure (or multistage decompression) in 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. Thereafter, the gas-liquid separator 35 recovers the liquefied gas to the liquefied gas storage tank 10, and the gas combustion device 232 through the ninth line L9 without discarding the flash gas generated in the gas-liquid separator 35. It can be supplied to and burned.

The second pressure reducing valve 342 depressurizes or expands the boil-off gas that is pressurized by the boil-off gas compressor 30 and heat-exchanged by the reliquefaction device 37 to liquefy at least a portion. For example, the second pressure reducing valve 342 can reduce the boil-off gas to 1 bar to 10 bar, and when the boil-off gas is liquefied and transferred to the liquefied gas storage tank 10, it can be reduced to 1 bar. The cooling effect can be achieved.

Here, the boil-off gas pressurized by the boil-off gas compressor (30) is cooled by heat exchange with the boil-off gas supplied from the liquefied gas storage tank (10) in the re-liquefaction device (37), but the pressure is discharged from the boil-off gas compressor (30). Can maintain discharge pressure. In this embodiment, the boil-off gas is depressurized by using the second pressure-reducing valve 342 to cool the boil-off gas, thereby liquefying the boil-off gas. At this time, as the pressure range to be depressurized increases, the cooling effect of the boil-off gas may increase. For example, the second pressure reducing valve 342 may reduce the boil-off gas pressurized to 300 bar by the boil-off gas compressor 30 to 1 bar.

The second pressure reducing valve 342 may be formed of 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, at least some of the boil-off gas can be liquefied by effectively cooling the boil-off gas through decompression. In this case, the expander may also be formed of an expander (not shown).

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

The second pressure reducing valve 342 is pressurized in the boil-off gas compressor 30 together with the aforementioned first pressure-reducing valve 341 to decompress the boil-off gas heat-exchanged in the reliquefaction device 37 in multiple stages, or (30) It is possible to decompress the boil-off gas supplied by branching to the intermediate stage in multiple stages, which can be flexibly applied through a change in 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 customer 20. In the present invention, the customer 20 may be a high pressure customer 21 and a low pressure customer 22, and the pressure of the liquefied gas required for each customer 20 may be different. As mentioned above, the boosting pump 40 ) And a high-pressure pump 41, may be composed of only the boosting pump 40 or only the high-pressure pump 41, and may be provided in various 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 customer 20, and the present invention is not particularly limited thereto.

In this case, each of the boosting pump 40 and the high pressure pump 41 may be provided in plural, and one pump may be used as a main and the other pump may be used as a backup. Of course, more than one pump can be driven simultaneously to lower the load.

Lines (first and sixth lines; L1, L6, etc.) 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. I can. At this time, the lines (L1, L6) supplying the liquefied gas are connected to the vaporizer 42 and/or the customer 20, which will be described later, so that the liquefied gas is transferred from the liquefied gas storage tank 10 to the customer 20. have.

Lines (L1, L6) for supplying liquefied gas are a high-pressure liquefied gas supply line (first line; L1) connected from the liquefied gas storage tank 10 to the high-pressure consumer 21 through pumps 40 and 41 It may and/or may be a low-pressure liquefied gas supply line (6th line; L6) connected from the liquefied gas storage tank 10 to the low-pressure consumer 22 through 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. In addition, the branch point may be determined in various ways according to the required pressure of the customer 20 (for example, between the boosting pump 40 and the high pressure pump 41).

The vaporizer 42 heats the liquefied gas. The liquefied gas stored in the liquefied gas storage tank 10 is at a cryogenic temperature of about -160 degrees, and the required temperature of the liquefied gas required by the customer 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 by 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 vaporization fruit storage tank 421, a vaporization fruit circulation pump 422, a vaporization fruit supply device 423, and a vaporization heat exchanger 424.

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

The vaporized fruit circulation pump 422 is configured to supply vaporized fruit from the vaporized fruit storage tank 421 to the vaporization heat exchanger 424, and a plurality of vaporized fruit may be provided and connected in parallel or in series, and when the vaporized fruit is a 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 vaporization fruit can be cooled while heating the liquefied gas in the vaporization heat exchanger 424, it is necessary to supplement heat to the cooled vaporization fruit. Accordingly, after the vaporization fruit is heated by steam or the like, the liquefied gas may be heated in the vaporization heat exchanger 424.

The vaporized fruit supply device 423 may include a first vaporized fruit supply device 4231 and a second vaporized fruit supply device 4232, and may be provided in plurality. Here, the vaporized nut first supply device 4231 and the vaporized nut second supply device 4232 may be jacket cooling water or sea water of the engine, 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 the vaporization heat exchanger 424, the vaporization fruit supply device 423, the vaporization fruit circulation pump 422, and the vaporization fruit storage tank 421. However, each component connected by the vaporized fruit circulation line (GL) (evaporation heat exchanger 424, vaporization fruit supply device 423, vaporization fruit circulation pump 422, and vaporization fruit storage tank 421) Unlike the drawings, the order of may be variously changed.

In addition, in the vaporization fruit circulation line GL, the vaporization fruit branch lines GLb, GBL1, and GBL2 bypass the vaporization fruit supply device 423 to properly control the temperature of the vaporization fruit supplied to the vaporization heat exchanger 424. ) Can be connected, and the vaporized fruit branch lines GLb, GBL1, GBL2 are branched from the vaporized fruit circulation line GL at the upstream of the vaporized fruit supply device 423, and the vaporized fruit branching line GL is downstream of the vaporized fruit supply device 423. It may be merged into the circulation line GL.

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

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 a low-pressure liquefied gas supply configuration provided in the low-pressure liquefied gas supply line (6th 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 configuration for supplying the low-pressure liquefied gas may be provided together with the configuration for supplying the high-pressure liquefied gas, or may be provided alone, and it is not particularly limited because it may vary in various ways according to the configuration of the customer 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 are shared and may be branched downstream of the boosting pump 40.

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

The forced vaporizer 50 may be connected to the low-pressure liquefied gas supply line L6, and vaporize the liquefied gas and transmit it to the low-pressure consumer 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 liquefied gas, the driving efficiency may be lowered. Accordingly, according to the present invention, by separating heavy carbon that vaporizes the liquefied gas and maintains the liquid phase, the quality of the liquefied gas supplied to the customer 20 can be improved, thereby increasing the driving efficiency of the customer 20.

At this time, the gas-liquid separator 51 may be referred to as a mist separator, a heavy carbon separator, and the like, and the liquid heavy carbon may be returned to the liquefied gas storage tank 10 or delivered to a separately provided tank. 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 is separated. The forced vaporizer 50 heats the liquefied gas, but the vaporized liquefied gas has a temperature (for example -100 degrees) to retain the heavy carbon in a liquid state, so it may not reach the temperature required by the customer 20 .

Accordingly, the heater 52 may heat the liquefied gas using various heat sources, similar to the forced vaporizer 50, and the heat source may be shared with the forced vaporizer 50 and/or the vaporizer 42.

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

Liquefied gas is stored in the liquefied gas storage tank 10, but foreign substances may be mixed into the liquefied gas inside the liquefied gas storage tank 10 by various fluids returned from the outside. Therefore, the strainer can filter out foreign substances mixed with 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 to about -100 degrees, and this is to remove heavy carbon as described above. At this time, the forced vaporizer 50 is provided with a liquefied gas controller (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 may be adjusted. .

The gas supply unit in the present 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 for compressing the boil-off gas generated in the liquefied gas storage tank 10 to the outside during bunkering or for incineration, and the type of the compressor is not limited.

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

The reliquefaction device 37 supplies cold heat to reliquefy the boil-off gas through the reliquefaction refrigerant supply device, and the refrigerant supplied from the reliquefaction refrigerant supply device is transferred to the reliquefaction heat exchanger through a separate pump (not shown). It can be supplied to supply cold heat to the boil-off gas to re-liquefy.

The return pump 38 converts the liquid phase to the liquefied gas storage tank 10 through the tenth line L10 from the gas-liquid separator 35 for separating 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 (the supply of the liquid phase is due to the pressure difference between the gas-liquid separator 35 and the liquefied gas storage tank 10) When stopped), the liquid phase of the gas-liquid separator 35 is supplied to the liquefied gas storage tank 10 through the eleventh line (L11) and bypass valves (not shown), which are bypass lines, and the return pump 38. I 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 will be supplied to the liquefied gas storage tank 10 through the tenth line L10. In the case where the liquid boil-off gas stored in the first gas-liquid separator 35 is stored at a pressure lower than the internal pressure of the liquefied gas storage tank 10, the liquefied gas storage tank ( 10) can be supplied.

Hereinafter, an embodiment of a gas treatment system that can be derived through each of the above-described configurations will be described.

The gas treatment system 1 according to the exemplary 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 it to the customer 20.

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

First, looking at the processing mechanism of the liquefied gas stored in the liquefied gas storage tank 10, the gas treatment system 1 according to the embodiment of the present invention, the liquefied gas stored in the liquefied gas storage tank 10 is transferred to the first line (L1). ) To the consumer 20, first pressurization using a boosting pump 40, and then filter impurities of 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) 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 to be vaporized at least in part, and the forced vaporized liquefied gas is supplied to the gas-liquid separator 51 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 has been 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 and vaporized by the carburetor 42 and then supplied to the high pressure consumer 21. I can.

Looking at the processing mechanism of the boil-off gas generated in the liquefied gas storage tank 10, the gas treatment system 1 according to the embodiment of the present invention, c) the second boil-off gas generated in the liquefied gas storage tank 10 Along the line L2 or d) the third line L3, the boil-off gas compressor 30 may be used to pressurize multiple stages and supply it to the customer 20.

c) The boil-off gas supplied through the second line (L2) can be multi-stage compressed to high pressure by the boil-off gas compressor (30) and supplied to the high-pressure consumer (21). The vaporized liquefied gas may also be joined and supplied to the high pressure consumer 21 together.

d) The boil-off gas supplied through the third line (L3) is the boil-off gas supplied by the boil-off gas supplied through the second line (L2) branched from the second or third stage of the boil-off gas compressor (30), It may be supplied to the low pressure consumer 22, and may be supplied to the low pressure consumer 22 by joining the liquefied gas forcibly vaporized through the process of a) described above.

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

Of course, the boil-off gas generated from 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 to the vent mast 24 through a valve (not shown) provided on the line.

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

The boil-off gas generated in the liquefied gas storage tank 10 of the embodiment of the present invention is supplied to the boil-off gas consumer 20 when the internal pressure of the liquefied gas storage tank 10 is more than a preset pressure, and the liquefied gas storage tank 10 If the internal pressure of) is less than the preset pressure, it is accumulated in the liquefied gas storage tank 10. Here, the preset pressure may be 1.06bar to 1.12bar, 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 propulsive force of the ship (not shown) may be stopped, or it may be a case of bunkering, anchoring, or ballast voyage.

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 in the liquefied gas storage tank 10 The liquefied gas storage tank 10 can be compressed as it is.

In an embodiment of the present invention, when the internal pressure of the liquefied gas storage tank 10 is higher than a 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 by the boil-off gas compressor (30) to supply the boil-off gas to the gas combustion device (23), 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 from the liquefied gas storage tank 10 is supplied to the 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 from 10) can 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. There is no power consumption, and there is an effect of preventing waste of boil-off gas because it does not emit boil-off gas to the outside.

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

The gas treatment system 1 according to an embodiment of the present invention includes an H/D compressor 36 for pressurizing the boil-off gas generated in the liquefied gas storage tank 10, and the evaporation compressed by the H/D compressor 36. A heater (not shown) that heats the gas and temporarily stores the boil-off gas generated in the liquefied gas storage tank 10 when bunkering or the onshore storage tank 10 in which the liquefied gas to be supplied to the liquefied gas storage tank 10 is stored. It includes a temporary storage (not shown) as a major component.

When liquefied gas is initially loaded into the liquefied gas storage tank 10 from outside (including when liquefied gas is shipped after maintenance work of the liquefied gas storage tank 10 is completed), that is, when bunkering, liquefied gas Considering that is a cryogenic combustible 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 to eliminate the possibility of fire or explosion, an inert gas is supplied to the liquefied gas storage tank 10. ) To remove oxygen. Thereafter, the hydrocarbon gas is supplied into the liquefied gas storage tank 10 to remove the inert gas, and a cool-down process of cooling the liquefied gas storage tank 10 by using the liquefied gas proceeds. . When the cooling down process is completed, the replacement method is completed, and then, liquefied gas such as LNG is supplied to the inside of the liquefied gas storage tank 10 to perform shipping.

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

First, all of the liquefied gas stored in the liquefied gas storage tank 10 is discharged to the shore. At this time, the remaining liquefied gas is present, and a warm-up step is performed to remove all the remaining liquefied gas. The warm-up step is to increase 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 and heating it with a separate heater and returning it to the liquefied gas storage tank 10. Let all remaining liquefied gas vaporize. After the warm-up step, an inert gas is supplied to remove all the remaining boil-off gas in the liquefied gas storage tank 10, and after drying the inside by introducing a drying gas, oxygen is supplied to supply air therein. By passing through the above process, the unloading process of the liquefied gas storage tank 10 is completed, and thereafter, an operator for performing maintenance work, etc. becomes available.

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 increases. 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 warming up step, a compressor is used in the process of compressing the boil-off gas 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 a shore customer (Shore), or warms up when the liquefied gas is unloaded (before maintenance of the liquefied gas storage tank 10). In the step, the boil-off gas remaining in the liquefied gas storage tank 10 is pressurized and returned to the liquefied gas storage tank 10 so that the boil-off gas is circulated to the liquefied gas storage tank 10.

Specifically, the H/D compressor 36 may receive and compress the boil-off gas generated from the liquefied gas storage tank 10 through the seventh line L7 during bunkering and supply it to a shore customer, When the liquefied gas is unloaded (when the liquefied gas storage tank 10 is maintained before maintenance), the boil-off gas remaining in the liquefied gas storage tank 10 is compressed and heated with a heater 361, and then the 8th line (L8) and By returning to the liquefied gas storage tank 10 through the 12th line (L12), the boil-off gas is returned to the liquefied gas storage tank 10, the H/D compressor 36, the heater 361, the liquefied gas storage tank 10 It can be cycled in order. Accordingly, all of the liquefied gas stored in the liquefied gas storage tank 10 can be vaporized, and all of the vaporized liquefied gas can be discharged to the outside of the liquefied gas storage tank 10.

At this time, the H/D compressor 36 may be a high duty type compressor.

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

As described above, in the embodiment of the present invention, since the H/D compressor 36 can be used for bunkering, liquefied gas unloading, or liquefied gas storage tank 10 maintenance, the construction cost of the compressor is reduced. In addition, the space used in the ship is maximized by reducing the construction space of the system.

The gas treatment system 1 according to the embodiment of the present invention further includes a decompression valve 341 along with the reliquefaction device 37 to improve the reliquefaction rate, and a return pump according to the internal pressure of the gas-liquid separator 35 35) and a technology for sharing a line through which boil-off gas is supplied to the GCU 23 and the reliquefaction device 37 may be included.

The gas treatment system 1 according to an embodiment of the present invention includes a boil-off gas compressor 30 that pressurizes the boil-off gas generated in the liquefied gas storage tank 10 in multiple stages, and the boil-off gas compressed by the boil-off gas compressor 30. The reliquefaction device 37 that liquefies through a refrigerant, a first pressure reducing valve 341 that depressurizes or expands the boil-off gas compressed by the boil-off gas compressor 30, and at least partially liquefied boil-off gas through the re-liquefaction device The main configuration includes a gas-liquid separator 35 that maintains a second depressurized pressure of the reliquefied boil-off gas through the second pressure reducing valve 342 and the second pressure reducing valve 342 that expands, and separates the gas and liquid phases. do.

Here, the re-liquefaction device 37 may liquefy the boil-off gas that is branched from the middle end of the boil-off gas compressor 30 and compressed to a low pressure (13 bar to 15 bar) through the refrigerant, and more specifically, the boil-off gas compressor ( The boil-off gas branched at the middle end of 30) and compressed to a low pressure (13bar to 15bar) is first reduced to 7bar to 8bar through the first pressure reducing valve 341 and then cooled through the reliquefaction device 37, The cooled boil-off gas may be secondarily reduced 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 device 37 to further improve the reliquefaction efficiency compared to the prior 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 be restored. In an embodiment of the present invention, a return line (L10; line 10) connecting the gas-liquid separator 35 and the liquefied gas storage tank 10, and a bypass line L11 bypassed on the return line L10; 11 line), a pump 38 (return pump) and a first pressure reducing valve 341 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 branch line (not shown) branched between the reliquefaction device 37 and supplied to the gas combustion device 23 may be further included.

Specifically, the liquid liquefied gas stored in the gas-liquid separator 35 is transferred to the liquefied gas storage tank 10 through a return line (L10; line 10) when the internal pressure of the gas-liquid separator 35 is higher than a preset pressure value. 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; line 11). have.

That is, since the gas-liquid separator 35 stores the secondary depressurized evaporation gas at 5 to 6 bar through the second pressure reducing valve 342, the evaporated gas in the liquid phase is physically higher than the internal pressure of the liquefied gas storage tank 10. Since it can be naturally supplied through the pressure gradient, which is the law, when the internal pressure of the gas-liquid separator 35 is greater than or equal to a preset pressure value, the return pump 38 is supplied 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, the branch line is branched at the intermediate stage of the boil-off gas compressor 30 and is branched at the intermediate stage of the boil-off gas compressor 30 and compressed at a low pressure when the supply amount of boil-off gas compressed to a low pressure is greater than a preset supply amount. When at least part of the boil-off gas is supplied to the gas combustion device 23, and the supply amount of the boil-off gas branched at the intermediate stage of the boil-off gas compressor 30 and compressed to a low pressure is less than a preset supply amount, the boil-off gas compressor 30 It is possible to supply all of the boil-off gas that is branched at the middle end of and compressed to a low pressure to the reliquefaction device 37.

That is, the first pressure reducing valve 341 and the second pressure reducing valve 342 are provided on the fourth line L4 together to provide a side stream line of a separate boil-off gas compressor 30 in addition to the fourth line L4. Since there is no need to do so, it is possible to minimize the branching lines of the boil-off gas compressor 301, thereby improving the driving reliability of the system. (When the number of side stream lines of the evaporative gas compressor 30 increases, driving efficiency increases. Drop)

Here, the preset pressure value is 5 bar to 6 bar, the reliquefaction device 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 liquefied gas to the low pressure consumer 22 and supplying the liquefied gas to the high pressure consumer 21 without a separate depressurization. It may include skills that can be made.

The gas treatment system 1 according to the embodiment of the present invention includes a boosting pump 40 for first pressurizing the liquefied gas stored in the liquefied gas storage tank 10, and the liquefied gas first pressurized from the boosting pump 40. A high-pressure pump 41 that receives and secondarily pressurizes a vaporizer 42 that receives and vaporizes the secondly pressurized liquefied gas from the high-pressure pump 41, a high-pressure liquefied gas or boil-off gas compressor 30 vaporized from the vaporizer 42 ), a high-pressure consumer (21) that receives and consumes pressurized boil-off gas from the evaporative gas compressor (30), a low-pressure consumer (22) that receives and consumes the boil-off gas pressurized to a low pressure and consumes it, a liquefied gas storage tank (10) It is provided between the forced vaporizer 50 for forcibly vaporizing the liquefied gas stored in (10) and the forced vaporizer 50 and the low pressure consumer 22, and receives the forcibly vaporized liquefied gas from the forced vaporizer 50 It includes a gas-liquid separator 51 for separating into a liquid phase 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 vaporizer 50, and the high pressure pump 41 through the boosting pump 40 ) And the use of a pump supplied to the forced carburetor 50 can be shared.

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

In addition, 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 and vaporizes it, and then supplies it to the front end of the boil-off gas compressor 30. I can. In the embodiment of this case, since the required pressure of the customer 20 is matched by the boil-off gas compressor 30, there is an effect of lowering the delivery pressure of the boosting pump 40. Of course, even in this case, the liquefied gas supplied to the forced vaporizer 50 may be supplied through the boosting pump 40 that supplies the liquefied gas to the high pressure pump 41.

In this way, by sharing the use of the pump supplied to the high-pressure pump 41 and the forced vaporizer 50 through the boosting pump 40, there is an effect of reducing the construction cost of the pump 40, and the forced vaporizer 50 By supplying the forcible boil-off gas that has passed through) to the front end of the boil-off gas compressor 30, the liquefied gas delivery pressure in the liquefied gas storage tank 10 is lowered, thereby reducing the driving power of the pump 40.

The gas treatment system 1 according to the embodiment of the present invention includes a return line L10 of a gas-liquid separator 35 provided at a rear end of the reliquefaction device 37, and a cool-down circulation line L13 of the high pressure pump 42. , A technology for 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 may be included.

The gas treatment system 1 according to the embodiment of the present invention is a reliquefaction device 37 for reliquefying the boil-off gas compressed by the boil-off gas compressor 30, and vaporization of the boil-off gas reliquefied by the reliquefaction device 37. Vaporized liquefied gas forcibly vaporized from the gas-liquid separator 35 for separating into a liquid phase, a high pressure pump 42 for pressurizing the liquefied gas stored in the liquefied gas storage tank 10, and a forced vaporizer 50 for forcibly vaporizing the liquefied gas. The gas-liquid separator 51 for separating into a liquid phase, a cool-down circulation line (L13; line 13) connected to the liquefied gas storage tank 10 from the high-pressure pump 42 when the high-pressure pump 42 cools down, the gas-liquid separator The return line (L10; line 10) 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 to the liquefied gas storage tank 10 It includes a return line (not shown) of the gas-liquid separator 51 as a main configuration.

In an embodiment of the present invention, when the high pressure pump 41 is cooled down, the line L13 returning from the high pressure pump 41 to the liquefied gas storage tank 10, the liquid phase of the gas-liquid separator 35 is 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.

In this way, the structure of the return line is simplified by sharing 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). As a result, the driving reliability of the system is improved, the return is stably implemented, and the return line is shared so that a cooldown can be performed in advance, so that the liquid boil-off gas is recovered while returning to the liquefied gas storage tank (10). There is an effect of not occurring, that is, there is an effect of increasing the actual reliquefaction efficiency.

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

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 boil-off gas is reliquefied by the reliquefaction 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 on the shared line and effectively share the return line. (The reliquefaction device 37 is driven. In this case, the boil-off gas remains. In this case, since a sufficient amount of boil-off gas is supplied to the high-pressure consumer 21 through the boil-off gas compressor 30, the liquefied gas is supplied through the high-pressure pump 41. There is no need to send it to 21), so there is no case that 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 consumer 21 and the low-pressure consumer 22 are driven. Can be.

The forced carburetor 50 operates only when the low pressure consumer 22 is driven, and the high pressure pump 41 is operated only when the high pressure consumer 21 is driven, so that the high and low pressure consumer 21 and 22 Only when both 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.

Due to this, the return line of the gas-liquid separator 51 is pre-cooled due to the cool-down of the high-pressure pump 41, and the liquid phase returned from the gas-liquid separator 51 to the liquefied gas storage tank 10 is not regasified, and thus the liquefied gas storage tank (10) The internal pressure 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 have different flow points so that there is no problem of back pressure. (Cooldown of the high-pressure pump 41 is It is driven only at the initial stage 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 consumer 22.)

The gas treatment system 1 according to the embodiment of the present invention provides a technology for simplifying the cooling down of the return line of the gas-liquid separator 51 by connecting the front end of the forced vaporizer 50 with the return line of the gas-liquid separator 51. Can include.

The gas treatment system 1 according to the embodiment of the present invention includes a gas-liquid separator 51 for separating the liquefied gas forcibly vaporized from the forced vaporizer 50 for forcibly vaporizing the liquefied gas into a gas phase and a liquid phase, and a gas-liquid separator 51 A return line of the gas-liquid separator 51 for returning the liquid phase of the liquefied 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) It includes as the main composition.

In an 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 You can share lines together.

Through this, by connecting the bypass line of the forced vaporizer 50 to the return line of the gas-liquid separator 51, not the front end of the gas-liquid separator 51, the bypass function of the forced vaporizer 50 and the return line of the gas-liquid separator 51 Since the cool-down function can be shared, 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 for supplying a heat source to glycol water used in the vaporizer 42 in parallel and serially supplying engine coolant and steam.

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

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

The first and second embodiments 42a and 42b of the vaporizer of the gas treatment system 1 according to the exemplary embodiment of the present invention are vaporizers 424 for vaporizing the liquefied gas stored in the liquefied gas storage tank 10 through a vaporized fruit. ; Evaporation heat exchanger), a first heat exchanger (4231; first supplying device for vaporized fruit), a second heat exchanger (4232; second supplying device for vaporized fruit) and vaporization for heat exchange between the vaporized fruit and engine coolant It includes a circulation pump 422 to circulate to supply the fruit to the vaporizer 424.

Specifically, in the first and second embodiments 42a and 42b of the vaporizer of the gas treatment system 1 according to the exemplary embodiment of the present invention, the vaporized nut first supply device 4231 and the vaporized nut 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, and more specifically, the circulation pump 422, the vaporized fruit first supply device ( 4231), the vaporized fruit second supply device 4232 may be connected in series in that 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.

Here, in the first vaporized fruit supply device 4231 and the second vaporized fruit supply device 4232, the first vaporized fruit supply device 4231 is a plate method, and the second vaporized fruit supply device 4232 is a Shell&Tube method. So that the types of heat exchangers may be different from each other. Of course, the two heat exchangers can be used in the same type as the plate method or the shell&tube method. In addition, the second vaporized fruit 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 exemplary embodiment of the present invention, the first supply of vaporized fruit is connected by connecting the front end and the rear end of the first vaporized fruit supply device 4231 A first bypass line (GBL1; first branch line of vaporized fruit) for bypassing the vaporized fruit passing through the device 4231 from the rear end to the front end of the vaporized fruit first supply device 4231, and a second vaporized fruit supply device 4232 ), a second bypass line (GBL2; vaporized fruit agent) for bypassing the vaporized fruit passing through the vaporized fruit second supply device 4232 from the rear end to the front end of the vaporized fruit second supply device 4232 The second branch line) and a control unit 902 that controls the first bypass line GBL1 or the second bypass line GBL2, and a vaporized fruit storage tank 421 for storing the vaporized fruit may be further included.

The control unit 902, when the vaporized fruit supplied to the vaporizer 424 is less than or equal to a preset temperature value, drives the vaporized fruit first branch line GBL1 or the second branch line GBL2 to reheat the vaporized fruit. I can. Here, the preset temperature value is from 85 degrees to 95 degrees, and the second vaporized fruit supply device 4232 may supply a heat source depending on the heat source supply capability of the first vaporized fruit supply device 4231.

When describing the process of heating/cooling circulation of the vaporized fruit in the first embodiment 42a of the vaporizer of the gas treatment system according to an embodiment of the present invention, the vaporized fruit stored in the vaporized fruit storage tank 421 is circulating the vaporized fruit. It is circulated through the pump 422 and heated by the engine coolant (jacket cooling water) by the first vaporized nutrient supply device 4231 to be heated to a maximum image of 70 degrees, and then the second vaporized nutrient 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 and flowing through the first line (L1) below zero. The liquefied gas of 130 degrees can be heated to an image of 35 to 55 degrees, and the vaporized refrigerant can be cooled from an image of 90 degrees to an image of 50.

Here, the engine coolant is supplied by the first vaporized nutrient supply device 4231, and when heated, the amount of engine coolant varies according to the driving of the engine, so when the engine coolant is driven at a low speed, the amount of heat source supplied to the engine coolant can be reduced. The heating operation may be performed by varying dependently on the vaporization fruit first supply device 4231. This can be implemented by driving the above-described control unit 902, and the control unit 902 receives temperature information of the liquefied gas or the 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 vaporizer of the gas treatment system 1 according to an embodiment of the present invention, in the second embodiment 42b, the heating/cooling cycle of the vaporized fruit will be described.The vaporized fruit first supply device 4231 and the vaporized fruit circulation pump Since only the order of (422) has been changed, other than that, it is the same as that described in the first embodiment 42a of the vaporizer described above, so this will be replaced.

Hereinafter, a description will be made of the third embodiment of the vaporizer 42c.

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

The third embodiment 42c of the vaporizer of the gas treatment system 1 according to the embodiment of the present invention includes a vaporization heat exchanger 424, a vaporization heat first supply device 4231, a vaporization fruit second supply device 4232, Circulation pump 422, a heater 423 (additional heater for vaporized fruit) and vaporized fruit 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 A bypass line (GBL4) provided at the rear end of the first supply device 4231 and configured to supply the vaporized fruit heated in the first supply device 4231 to the front end of the second supply device 4322. A third branch line).

In the vaporized fruit first supply device 4231 and the vaporized fruit second supply device 4232, 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 vaporized fruit second supply device 4232 can heat the vaporized fruit sub-optimally, 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 heats the vaporized fruit through the heater 423 when the temperature at the rear end of the vaporized fruit first supply device 4231 is below a preset temperature. Alternatively, it may be supplied to the front end of the vaporized fruit second supply device 4232 through the bypass line GBL4.

Here, the vaporized nut first supply device 4231 is a plate method, and the vaporized nut second supply device 4232 is a shell&tube method, and the types of the two heat exchangers may be different, and of course, the two heat exchangers are a plate method or a shell&tube method. It can also 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.

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

However, since the amount of the 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 a severe temperature change. In order to prevent this, in the present invention, an additional heater 423 may be further provided. In the present invention, when the engine is driven at a low speed and the amount of heat source supplied to the engine coolant is reduced, it is possible to heat the image to 90 degrees by reheating through the additional vaporization heater 423. Thereafter, the liquefied gas of -130 degrees Celsius, which is supplied to the vaporization heat exchanger 424 and flows through the first line L1, can be heated to an image of 35 to 55 degrees, and the vaporized refrigerant may be cooled from an image of 90 degrees to an image of 50. .

Here, the second vaporized nutrient supply device 4232 may be varied depending on the first vaporized nutrient supply device 4231 to perform heating operation. This can be implemented by driving the above-described control unit 902, and the control unit 902 receives temperature information of the liquefied gas or the 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, in the case where the driving of the engine is stopped for a long period of time and the supply of engine coolant is very low, and the amount of heating is not sufficient even with the additional heater for vaporizing fruit, the vaporized fruit second supply device 4232 is the third vaporized fruit. Since it is not supplied to the branch line GBL3 but is supplied to the vaporized fruit circulation line GL, the vaporized fruit can be heated up to 90 degrees.

In the carburetor according to an embodiment of the present invention, since the amount of engine coolant varies according to the driving of the engine, when the amount of heat source supplied to the engine coolant decreases when the engine coolant is driven at a low speed, the fourth branch line GBL4 ) Is bypassed to the second vaporized fruit supply device 4232, and heated up to 90 degrees by the second vaporized fruit supply device 4232.

In this way, the flow of steam is reduced by the engine coolant through the heating technology of the vaporized fruit through parallel or series connection of the vaporized fruit supply device described above, which reduces the boiler operation, thereby reducing fuel consumption, and serial or parallel connection. As a result, there is an effect of improving the driving reliability of the carburetor 42.

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

The gas treatment system 1 according to the embodiment of the present invention includes a boil-off gas compressor 30 provided in parallel, a liquefied gas treatment device that pressurizes/heats the liquefied gas stored in the liquefied gas storage tank 10 and supplies it to a customer. (40, 41, 42), a re-liquefaction device 37 for reliquefying the boil-off gas compressed by the boil-off gas compressor 30, a reliquefaction device 37 provided at the rear end of the re-liquefaction device 37 Mainly, a second pressure reducing valve 342 for depressurizing or expanding the evaporated gas, a gas combustion device 23 for consuming the evaporated gas, and a forced vaporizer 50 for forcibly vaporizing the liquefied gas stored in the liquefied gas storage tank 10. Included in the composition.

Here, the liquefied gas processing apparatus 40, 41, 42 receives a boosting pump 40 for primary pressurizing the liquefied gas stored in the liquefied gas storage tank 10, and the pressurized liquefied gas from the boosting pump 40 It includes a high-pressure pump 41 for secondary pressure and a vaporizer 42 that receives and vaporizes 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 a first boil-off gas. It may be provided with a compressor (not shown) and a second boil-off gas compressor (not shown).

Hereinafter, the first parallel driving of the gas processing 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 It is greater than 1,12 bar, the third preset pressure is less than the first preset pressure and greater than 1.06 bar, and the fourth preset pressure may be less 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 greater than or equal to the first preset pressure, a 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) are additionally driven.

The boil-off gas generated in the liquefied gas storage tank 10 may be supplied to the reliquefaction device 37 or the gas combustion device 23 when the internal pressure of the liquefied gas storage tank 10 is greater than or equal to the second preset pressure. , In addition to the case where the internal pressure of the liquefied gas storage tank 10 is greater than or equal to the second preset pressure, the liquefied gas processing devices 40, 41, and 42 may be additionally driven when the fuel requirement of the customer 20 is more than the preset required amount. 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 the internal pressure of the liquefied gas storage tank 10 is less than the fourth preset pressure , The internal pressure of the liquefied gas storage tank 10 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 Can be raised.

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

As described above, in an embodiment of the present invention, by driving the boil-off gas compressor 30 and the liquefied gas processing devices 40, 41, and 42 in parallel so that the driving of the customer 20 can be made elastically without supply of oil, There is an effect of reducing the system construction cost.

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

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

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

The boil-off gas compressor 30 is basically driven at a first preset pressure, and when the amount of boil-off gas generated in the liquefied gas storage tank 10 is greater than the fuel required amount of the customer 20, the re-liquefaction device 37 When the additional operation is performed and the amount of boil-off gas generated in the liquefied gas storage tank 10 is less than the required amount of fuel of the customer 20, the liquefied gas treatment devices 40, 41, and 42 and the oil treatment device may be additionally operated. . Preferably, the liquefied gas treatment apparatuses 40, 41, and 42 may be operated first, and the oil treatment apparatus may be operated next.

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, and the internal pressure of the liquefied gas storage tank 10 described above is changed according to the first preset pressure. On the other hand, it is possible to control the liquefied gas treatment devices 40, 41 and 42, the boil-off gas compressor 30, and the oil treatment device.

As described above, in the embodiment of the present invention, the boil-off gas compressor 30, the liquefied gas processing devices 40, 41, and 42, and the oil processing device are operated in parallel to satisfy the homeostasis of the fuel supply of the system, and thus the driving reliability of the system This has the effect of improving.

In the gas treatment system 1 according to the embodiment of the present invention, when the internal pressure of the liquefied gas storage tank 10 is high, the processing of liquefied gas, boil-off gas, and oil according to the flow of the internal pressure is implemented through parallel driving. May include technology.

The gas treatment system 1 according to the embodiment of the present invention includes a boil-off gas compressor 30 and a reliquefaction device 37 provided in parallel as main configurations. Here, the boil-off gas compressors 30 may be provided in parallel to include 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 greater than or equal to the preset pressure, the first boil-off gas compressor is operated and supplied to the customer 20, and the amount generated in the liquefied gas storage tank 10 is higher than the required amount of fuel from the customer 20. When the amount of boil-off gas is larger, the reliquefaction device 37 may be additionally operated or a second boil-off gas compressor may be additionally operated. Preferably. By first operating the second boil-off gas compressor and supplying it to the customer 20, it is possible to increase the speed of the ship, and the reliquefaction device 37 may be operated next. At this time, the preset pressure may be 1.11bar to 1.13bar.

As described above, in the embodiment of the present invention, the boil-off gas compressor 30 is driven in parallel and the reliquefaction device 37 is additionally driven to efficiently process the boil-off gas 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 explaining the present invention in detail, and the present invention is not limited thereto, and within the technical scope of the present invention, those of ordinary skill in the art It would be clear that the transformation or improvement is possible.

All simple modifications to changes of the present invention belong to 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 pressure consumer
22: low pressure consumer 23: gas combustion system (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: 1st to 13th line GL: Vaporized fruit circulation line
GLb: vaporized fruit branch line GBL1: vaporized fruit first branch line
GBL2: second branch line of vaporized fruit GBL3: third branch line of vaporized fruit
GBL4: Vaporized fruit fourth branch line

Claims (7)

A vaporizer that vaporizes the liquefied gas stored in the liquefied gas storage tank through a vaporized fruit and delivers it to the engine;
A first heat exchanger for exchanging heat between the vaporized fruit and engine coolant of the engine; And
And a second heat exchanger supplying a heat source to the vaporized fruit,
A vaporized fruit circulation line provided with the second heat exchanger and supplying the vaporized fruit to the vaporizer;
A vaporized nutrient branch line branched upstream of the second heat exchanger of the vaporized nutrient circulation line to join the downstream of the second heat exchanger of the vaporized nutrient circulation line and provided with the first heat exchanger; And
And a bypass line branched from the downstream of the first heat exchanger of the vaporized nutrient branch line and joined upstream of the second heat exchanger of the vaporized nutrient circulation line,
The first heat exchanger heats the vaporized fruit by using the engine coolant whose amount varies according to the driving of the engine,
The second heat exchanger heats the vaporized fruit using steam or sea water,
The first heat exchanger and the second heat exchanger,
The vaporization fruit is independently heated in parallel and then transferred to the vaporizer, or the vaporized fruit is sequentially heated in series and then delivered to the vaporizer to supply the vaporized fruit to the vaporizer to a constant heat source having a preset temperature. A gas treatment system, characterized in that. The method of claim 1,
Further comprising a heater provided at a rear end of the first heat exchanger and additionally heating the vaporized fruit heated in the first heat exchanger,
The vaporized fruit heated by the first heat exchanger,
When the temperature at the rear end of the first heat exchanger is less than or equal to a preset temperature, the vaporized fruit is heated through the heater. The method of claim 1,
The vaporized fruit heated by the first heat exchanger,
When the temperature at the rear end of the first heat exchanger is less than or equal to a preset temperature, the gas treatment system is supplied to the front end of the second heat exchanger through the bypass line. The method of claim 1,
Further comprising a circulation pump for circulating to supply the vaporized fruit to the vaporizer,
The first heat exchanger and the second heat exchanger,
Gas treatment system, characterized in that disposed at the rear end of the circulation pump. The method of claim 1, wherein the first heat exchanger and the second heat exchanger,
Gas treatment system, characterized in that the type of heat exchanger is different. The method of claim 1, wherein the first heat exchanger and the second heat exchanger,
Gas treatment system, characterized in that the type of heat exchanger is the same. delete

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