KR101842324B1 - Treatment system of gas - Google Patents

Abstract

A gas processing system according to an embodiment of the present invention includes: an evaporative gas compressor for multi-stage pressurizing evaporative gas generated in a liquefied gas storage tank and supplied with evaporative gas at room temperature; A BOG-BOG heat exchanger for exchanging heat between the evaporated gas compressed by the evaporative gas compressor and the evaporated gas supplied from the liquefied gas storage tank; And a heater for further heating the evaporation gas supplied from the liquefied gas storage tank heated by the BOG-BOG heat exchanger, wherein when the BOG-BOG heat exchanger is not driven, evaporation gas supplied from the liquefied gas storage tank Is bypassed to the BOG-BOG heat exchanger, preheated by the heater, and then supplied to the evaporative gas compressor.

Description

Treatment system of gas

The present invention relates to a gas treatment system.

A ship is a means of transporting large quantities of minerals, crude oil, natural gas, or several thousand containers. It is made of steel and buoyant to float on the water surface. The thrust generated by rotation of the propeller ≪ / RTI >

Such a ship generates 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 is rotated, .

In recent years, however, LNG fuel supply systems for driving an engine using LNG as a fuel have been used in an LNG carrier carrying Liquefied Natural Gas (LNG) It is also applied to other ships.

Generally, it is known that LNG is a clean fuel and its reserves are more abundant than petroleum, and its usage is rapidly increasing as mining and transfer technology develops. This LNG is generally stored in a liquid state at a temperature of -162 ° C below 1 atm under the pressure of 1 atm. The volume of liquefied methane is about 1/600 of the volume of the gaseous methane in the standard state, Is 0.42, which is about one half of the specific gravity of crude oil.

However, the temperature and pressure required to drive demand can differ from the state of the LNG stored in the tank. Therefore, in recent years, research and development have been conducted on technologies for controlling the temperature and pressure of LNG stored in a liquid state and supplying it to customers.

In addition, when LNG is stored in a liquid state, some LNG is vaporized as boiling off gas (BOG) is generated due to heat penetration into the tank. In the past, in order to reduce the tank pressure, And simply discharged to the outside. In recent years, however, the necessity of development has been increasing for applications such as re-liquefaction of evaporation gas generated from the tank and supply to the customer.

It is an object of the present invention to provide a gas processing system for effectively supplying liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer.

A gas processing system according to the present invention includes: an evaporative gas compressor for multi-stage pressurizing evaporative gas generated in a liquefied gas storage tank and supplied with evaporative gas at room temperature; A BOG-BOG heat exchanger for exchanging heat between the evaporated gas compressed by the evaporative gas compressor and the evaporated gas supplied from the liquefied gas storage tank; And a heater for further heating the evaporation gas supplied from the liquefied gas storage tank heated by the BOG-BOG heat exchanger, wherein when the BOG-BOG heat exchanger is not driven, evaporation gas supplied from the liquefied gas storage tank Is bypassed to the BOG-BOG heat exchanger, preheated by the heater, and then supplied to the evaporative gas compressor.

Specifically, when the BOG-BOG heat exchanger is driven, the evaporation gas supplied from the liquefied gas storage tank may be supplied to the evaporative gas compressor by bypassing the heater.

Specifically, when the BOG-BOG heat exchanger is driven, the evaporated gas supplied from the liquefied gas storage tank may be first preheated in the BOG-BOG heat exchanger and secondarily preheated in the heater.

Specifically, the evaporative gas compressor may be composed of multi-stages, the front end may be an evaporative gas compressor for room temperature, and the rear end may be an evaporative gas compressor for cryogenic temperature.

Specifically, the BOG-BOG heat exchanger is branched at the intermediate stage of the evaporative gas compressor, and is supplied with the evaporated gas compressed at a low pressure to re-liquefy the low-pressure evaporated gas.

Specifically, an evaporative gas decompressor for decompressing or expanding the evaporated gas compressed in the evaporative gas compressor; And a gas-liquid separator for separating the evaporated gas re-liquefied through the evaporation gas decompressor into vapor or liquid.

Specifically, the BOG-BOG heat exchanger is capable of re-liquefying the high-pressure evaporation gas by receiving the multi-stage compressed evaporation gas at a high pressure from the rear end of the evaporation gas compressor.

Specifically, the heater or the BOG-BOG heat exchanger may preheat the evaporated gas discharged from the liquefied gas storage tank to a temperature within a range of 1 to 40 degrees, and supply the evaporated gas to the evaporative gas compressor.

Specifically, in the heater, the fruit may be steam.

Specifically, the BOG-BOG heat exchanger is not provided with a separate relusing device, and it is possible to re-liquefy the evaporated gas compressed by the evaporative gas compressor by exchanging heat with the evaporated gas supplied from the liquefied gas storage tank.

Specifically, the high pressure may be from 200 bar to 400 bar (absolute pressure).

Specifically, the evaporative gas compressor is composed of five stages, and the BOG-BOG heat exchanger is branched between the second stage and the third stage of the evaporative gas compressor and supplied with the evaporated gas compressed at a low pressure, .

The gas treatment system according to the present invention can effectively supply liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer to enhance system stability and reliability.

1 is a conceptual diagram of a gas processing system according to an embodiment of the present invention.
2A is a conceptual diagram of a vaporization system in the gas 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.
3A is a conceptual diagram of a gas processing system according to an embodiment of the present invention.
3B is a conceptual diagram of a gas processing system according to an embodiment of the present invention.
3C is a conceptual diagram of a gas processing system according to an embodiment of the present invention.
3D is a conceptual diagram of a gas processing system according to an embodiment of the present invention.

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

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

Hereinafter, the liquefied gas may be LPG, LNG, or ethane, and may be, for example, LNG (Liquefied Natural Gas), and the evaporation gas may refer to BOG (Boil Off Gas) such as natural vaporized LNG.

The liquefied gas can be referred to irrespective of the state change, such as liquid state, gas state, mixed state of liquid and gas, supercooled state, supercritical state, and the like. Further, the present invention is not limited to the liquefied gas to be treated, but may be a liquefied gas processing system and / or a vaporized gas processing system.

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

1, a gas processing system according to an embodiment of the present invention can be mounted on a ship such as an LNG carrier and includes a liquefied gas storage tank 10, a customer 20, an evaporative gas compressor 30, A boosting pump 40, a high-pressure pump 41, a vaporizer 42, and a forced vaporizer 50.

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

The embodiment of the present invention may further include first to thirteenth lines L1 to L13. Valves (not shown) can be provided on the respective lines, and the supply amount of the evaporative gas and / or the liquefied gas and / or various refrigerants can be controlled according to the opening degree of each valve.

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

The liquefied gas storage tank (10) may be mixed with a liquefied gas in a liquid state and an evaporated gas in a gaseous state. This is because the external heat is penetrated into the liquefied gas storage tank 10 and the liquefied gas is heated, so that the evaporated gas can be generated.

At this time, the evaporation gas causes an increase in internal pressure of the liquefied gas storage tank 10 as the flow rate increases. Therefore, the discharge is preferable for protecting the liquefied gas storage tank 10. Therefore, the present invention can appropriately discharge the evaporation gas in accordance with the pressure of the liquefied gas storage tank 10.

The discharged evaporated gas may be burnt by the gas combustion unit 23 or the like or may be supplied to the consumer 20 (engine, turbine, boiler, etc.) and consumed.

Alternatively, the evaporated gas discharged from the liquefied gas storage tank 10 is cooled to a boiling point or lower by the re-liquefier 37 or the like to be described later, and is liquefied in a gaseous state into a liquid state (same as liquefied gas, And returned to the liquefied gas storage tank 10).

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

The barrier portion may be provided on the inner side (adjacent to the liquefied gas) with respect to the heat insulating portion, and the heat insulating portion may be provided on the outer side (the side adjacent to the hull) with respect 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, a stand-alone type, a pressurized type, or the like.

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

When the liquefied gas storage tank 10 is a membrane type, the structure can be determined according to a conventionally well-known type such as Mark III, No. 96. When the liquefied gas storage tank 10 is a stand-alone type, The structure can be determined according to a type well known in the art. Of course, the structure of the heat insulating portion is not limited to the above example.

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

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

The consumer 20 may be configured to consume liquefied gas or the like (liquefied gas, evaporated gas, or flash gas) and generate or burn energy while consuming liquefied gas or the like.

For example, the customer 20 may be a low-pressure consumer 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 remelting device, a boiler, A high-pressure consumer using a liquefied gas having a pressure of about 200 bar to 400 bar (absolute pressure) such as a high-pressure engine (ME-GI engine, etc.), and the pressure of the liquefied gas required for each customer 20 may be different.

That is, in the present invention, the customer 20 comprehensively means all configurations consuming the liquefied gas and the like, and the present invention does not limit the customer 20 to a specific configuration.

In the embodiment of the present invention, the liquefied gas stored in the liquefied gas storage tank 10 or the gas supply unit for processing the evaporated gas is constituted. Here, the gas supply unit is a structure for delivering the liquefied gas and / or the evaporated gas to the customer 20 such as the engine, and includes the evaporation gas compressor 30, the boosting pump 40, the high pressure pump 41, the vaporizer 42, .

The evaporative gas compressor (30) compresses the evaporated gas discharged from the liquefied gas storage tank (10). The evaporation gas compressor 30 may be of a centrifugal type, a reciprocating type, etc., and a plurality of evaporative gas compressors 30 may constitute an evaporative gas compression unit (not shown).

In this case, the plurality of evaporative gas compressors (30) constituting the evaporative gas compression section may be provided so as to be both centrifugal, reciprocal, centrifugal and reciprocal.

For example, the evaporative gas compressor 30 may include a reciprocating compressor and / or a centrifugal compressor, and a reciprocating compressor and a centrifugal compressor may be provided in parallel. At this time, the discharge pressure of the reciprocating compressor and the centrifugal compressor is May be the same or different.

For example, in the present invention, the evaporative gas compressor (30) may be composed of two stages, three stages, five stages, six stages or the like in a centrifugal manner. Each stage is compressed only according to the requirements of the evaporating gas to be supplied according to the type of the customer 20, but the larger the number, the more the discharge pressure is relatively large.

Also, the evaporative gas compressor 30 may be configured as a cryogenic compressor for treating the evaporated gas at a low temperature state of about -100 degrees discharged from the liquefied gas storage tank 10. However, since the temperature of the evaporation gas may increase when the evaporation gas is compressed by the evaporation gas compressor 30, some of the evaporation gas compressors upstream of the multi-stage evaporation gas compressors included in the evaporation gas compression section are cryogenic compressors , And the remaining evaporative gas compressor downstream may be a room temperature compressor.

When the evaporation gas is compressed by the evaporation gas compressor 30 and the temperature of the evaporation gas is increased, the volume of the evaporation gas may increase together with the volume of the evaporation gas. This can cause an unnecessary load increase of the evaporative gas compressor 30 such that at least one of the evaporative gas compressors 30 and / or at least one of the evaporative gas compressors 30 is supplied with compressed evaporated gas An evaporative gas cooler 31 for cooling the gas may be provided.

The evaporative gas cooler 31 can cool the evaporative gas using various heat sources such as the evaporator gas cooler 31, Flash gas and the like can be used in various ways.

Between each end of the evaporative gas compressor (30), a buffer tank (not shown) may be provided in addition to the evaporative gas cooler (31). The buffer tank may be provided for constant supply of the evaporating gas flowing into each end of the evaporative gas compressor 30 and constant maintenance of the supply pressure.

The evaporated gas flowing into the evaporated gas compressor (30) can be heat-exchanged with the compressed evaporated gas. However, the evaporation gas flowing into the evaporation gas compressor 30 due to the heat exchange can be preheated, so that the evaporation gas compressor 30 can be composed of all the room temperature compressors.

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

For example, when the evaporated gas compressed in the evaporative gas compressor 30 is used in a low pressure consumer 22 such as a turbine, a low-pressure engine (DFDE, DFDG, XDF, etc.), a re-liquefier, a boiler, The pressure may be between about 1 bar to 10 bar (absolute pressure) and the pressure of the compressed evaporated gas when the compressed evaporated gas is used in a high pressure consumer 21, such as a high pressure engine (such as ME-GI) ).

Of course, the evaporative gas compressor (30) is provided in a multi-stage, and the evaporated gas compressed at a low pressure by a part of the evaporative gas compressor (30) is discharged to the outside of the evaporative gas compressor (30) And the evaporated gas, which is further compressed by the high pressure by the remaining evaporative gas compressor 30, is discharged to the outside of the evaporative gas compressor 30 and can be used in the high pressure consumer 21.

That is, in the evaporation gas compression unit having the evaporation gas compressor 30 provided in multiple stages, the pressure of the evaporation gas supplied to each customer 20, the number of the evaporation gas compressor 30, the degree of compression of the evaporation gas, But can be variously determined.

It is possible to supply the evaporative gas from the liquefied gas storage tank 10 to each consumer 20 in order to transfer the evaporated gas from the liquefied gas storage tank 10 to the low pressure consumer 22 or the high pressure consumer 21 via the evaporative gas compressor 30. [ (Second, third, fifth, seventh and eighth lines (L2, L3, L5, L7, L8, etc.)).

The supply line connected to the low pressure consumer 22 from the evaporative gas compressor (end or intermediate stage) may be a low pressure supply line (third line L3), and the evaporative gas compressor 30 (end or middle stage) The supply line connected to the high-pressure consumer 21 may be a high-pressure supply line (second line L2). Therefore, the supply line can be branched to the low-pressure supply line (third line L3) and the high-pressure supply line (second line L2) on the basis of the evaporative gas compressor 30.

The evaporation gas compressor 30 compresses the evaporation gas to a low pressure and supplies it to the low pressure consumer 22 along the low pressure supply line L3 when only a part of the evaporation gas compressor 30 provided in multiple stages is provided, The evaporation 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 evaporative gas compressor (30), part of the lubricant may not be used, and the remainder may be lubricant. For example, if the evaporative gas compressor 30 is provided in five stages, the first to third evaporative gas compressors do not use lubricating oil (the lubricating oil is not incorporated in the evaporating gas), and the fourth to fifth stages use lubricating oil (The lubricating oil is mixed into the evaporating gas). This is because, in the case of the high pressure stage, the pressure of the evaporation gas is changed to the high pressure, and thus the lubricant is required for the piston of the evaporation gas compressor 30 to be smoothly driven.

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

The first pressure reducing valve 341 can pressurize or expand the evaporation gas that is pressurized by the evaporation gas compressor 30 and supplied to the remelting device 37. Although not shown here, the first pressure reducing valve 341 can supply the evaporation gas pressurized by the evaporation gas compressor 30 to the gas combustion device 23 as well as the re-liquefier 37, .

The first pressure reducing valve 341 is provided together with the second pressure reducing valve 342 so that the evaporating gas pressurized by the evaporating gas compressor 30 can be decompressed or expanded at a multi-stage. For example, the first pressure reducing valve 341 may be configured such that the evaporation gas pressurized by the evaporation gas compressor 30 or the evaporation gas branched and fed to the middle end of the evaporation gas compressor 30 is firstly reduced or first expanded, And the evaporated gas that has been heat-exchanged in the re-liquefier 37 can be re-liquefied by secondary pressure reduction or secondary expansion through the second pressure reducing valve 342 again.

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

The gas-liquid separator 35 separates the gas from the decompressed or expanded vaporized gas in the first pressure-reducing valve 341 or the second pressure-reducing valve 342. In the gas-liquid separator 35, the evaporated gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas can be supplied to the gas combustion apparatus 23 as flash gas.

Here, the evaporation gas supplied to the gas-liquid separator 35 may be in a state of being decompressed and cooled by the first pressure reducing valve 341 or the second pressure reducing valve 342. For example, the evaporated gas in the evaporative gas compressor (30) may be multi-stage pressurized to have a pressure of 200 bar to 400 bar, and the temperature may be around 45 degrees. The evaporated gas heated to a temperature of about 45 degrees is recovered to the re-liquefier 37 via the first pressure reducing valve 341. The evaporated gas heat-exchanged in the re-liquefier 37 is again supplied to the second pressure reducing valve 342, . At this time, in the first pressure reducing valve 341 or the second pressure reducing valve 342, the evaporation gas is cooled by the reduced pressure and can have a pressure of about 1 bar and a temperature of about -162.3 degrees.

As described above, in the present embodiment, the evaporation gas supplied to the gas-liquid separator 35 is reduced in pressure (or multi-step pressure reduced) by 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 evaporated gas can be liquefied. Thereafter, the gas-liquid separator 35 recovers the liquefied gas to the liquefied gas storage tank 10 and supplies it to the gas combustion device 232 through the ninth line L9 without discarding the flash gas generated in the gas- To be burned.

The second pressure reducing valve 342 decompresses or expands the evaporated gas that has been pressurized by the evaporative gas compressor 30 and heat-exchanged in the remelting device 37 to liquefy at least a part thereof. For example, the second pressure reducing valve 342 can reduce the pressure of the evaporation gas to 1 to 10 bar, and the pressure of the evaporation gas can be reduced to 1 bar when the liquefied gas is transferred to the liquefied gas storage tank 10, The cooling effect can be achieved.

Here, the evaporated gas pressurized in the evaporative gas compressor (30) is cooled by heat exchange with the evaporated gas supplied from the liquefied gas storage tank (10) in the refueling device (37) The discharge pressure can be maintained. In this embodiment, the evaporation gas is cooled by using the second pressure reducing valve 342 to reduce the evaporation gas, thereby liquefying the evaporation gas. At this time, the greater the pressure range to be depressurized, the greater the cooling effect of the evaporated gas. For example, the second reduced pressure valve 342 can reduce the evaporated gas pressurized to 300 bar by the evaporated gas compressor 30 to 1 bar.

The second pressure reducing valve 342 may be a line Thompson valve. Alternatively, the second pressure reducing valve 342 may be made of an inflator (not shown). In the case of the Row Thompson valve, depressurization can effectively cool the evaporated gas so that at least some of the evaporated gas is liquefied. At this time, the inflator may also be made of an expander (not shown).

On the other hand, the inflator can be driven without using any extra power, and in particular, the efficiency of the gas processing system 1 can be improved by utilizing the generated power as electric power for driving the evaporative gas compressor 30. The power transmission may be accomplished by, for example, a gear connection or an electric conversion and the like.

The second pressure reducing valve 342 is connected to the first pressure reducing valve 341 so that the evaporating gas pressurized by the evaporating gas compressor 30 and heat-exchanged in the refueling device 37 is multi- It is possible to multi-stage decompression of the evaporated gas branched and supplied to the intermediate stage 30, which can be flexibly applied by changing the configuration according to each embodiment.

The boosting pump 40 and the high pressure pump 41 can pressurize the liquefied gas so as to bring the liquefied gas close to or close to the pressure demanded by the customer 20. In the present invention, the customer 20 may be a high-pressure consumer 21 and a low-pressure consumer 22. Since the pressure of the liquefied gas required for each consumer 20 may be different, the boosting pump 40 And the high-pressure pump 41, the booster pump 40 alone or the high-pressure pump 41 alone, or may be provided in various other ways. That is, the pressure of the liquefied gas pressurized by the pumps 40 and 41 can 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.

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

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

The lines L1 and L6 for supplying liquefied gas are connected to a high pressure liquefied gas supply line (first line: L1) connected to the high pressure consumer 21 via the pumps 40 and 41 from the liquefied gas storage tank 10 And may be a low pressure liquefied gas supply line (sixth line: L6) connected from the liquefied gas storage tank 10 via the pump 40 to the low pressure consumer 22. 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 in one liquefied gas supply line And the branching point can be variously determined 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. 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 customer 20, a temperature rise 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 can be raised, but this is not sufficient. Therefore, the vaporizer 42 can be used to separate liquefied gas from other heat sources (steam, glycol water, Exhaust, engine cooling water, electricity, etc.).

In order to supply a heat source to the vaporizer 42, the present invention may include a vaporization storage tank 421, a vaporization heat transfer circulation pump 422, a vaporization heat 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 the supplied amount of vaporized fruit.

The vaporizing material circulation pump 422 is configured to supply vaporized heat from the vaporized material storage tank 421 to the vaporization heat exchanger 424 and may be provided in parallel or in series, A heat source compressor (not shown) may be provided in place of the vaporizing heat circulation pump 422.

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

The vaporized fruit supplying device 423 may be provided with a plurality of vaporizing first supply devices 4231 and a second supply device 4232 for vaporizing heat. Here, the first vaporizer feeder 4231 and the second vaporizer feeder 4232 may be jacket cooling water or seawater, respectively, and may be configured in parallel or in series with each other.

At this time, the vaporized liquid flows along the vaporizing material circulating line GL for circulating the vaporizing heat exchanger 424, the vaporizing material supplying device 423, the vaporizing material circulating pump 422 and the vaporizing material storage tank 421 (Vaporization heat exchanger 424, vaporized fruit supply device 423, vaporized fruit circulation pump 422 and vaporized fruit storage tank 421) connected by the vaporized fruit circulation line GL, May vary in various ways.

GBL1 and GBL2 are provided in the vaporizing material circulation line GL so as to bypass the vaporizing material supply device 423 and appropriately regulate the temperature of the gasification heat supplied to the vaporizing heat exchanger 424, And the vaporized fruit branching lines GLb, GBL1 and GBL2 are branched from the vaporizing material circulating line GL upstream of the vaporizing material supplying device 423 and connected to the vaporizing material feeding device 423 downstream of the vaporizing material feeding device 423, Can be merged into the circulation line (GL).

The vaporizing heat exchanger 424 can supply a heat source to the liquefied gas flowing on the liquefied gas supply line L1 through the circulated vaporized liquid to vaporize the liquefied gas. The configuration of the vaporization heat exchanger 424 may employ various configurations of other heat exchangers such as a shell & tube, but is not limited thereto.

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 structure provided in the low-pressure liquefied gas supply line (sixth line L6) , 41), and the vaporizer 42 may be a high-pressure liquefied gas supply structure provided in the high-pressure liquefied gas supply line (L1).

The low-pressure liquefied gas supply structure may be provided together with the high-pressure liquefied gas supply structure, or may be independently provided, and is not particularly limited as it can be varied 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 can share booster pump 40. That is, the low-pressure liquefied gas supply line and the high-pressure liquefied gas supply line are at least partially shared and can be branched downstream of the boosting pump 40.

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

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

A gas-liquid separator 51 (which may be a heavy carbon separator) separates the residual heavy carbon from the vaporized liquefied gas into a liquid phase. The consumer 20 (preferably the low-pressure consumer 22) consuming the liquefied gas may lower the driving efficiency when a large amount of heavy carbon is introduced. Therefore, the present invention can increase the driving efficiency of the consumer 20 by improving the quality of the liquefied gas supplied to the consumer 20 by separating the heavy carbon which vaporizes the liquefied gas and maintains the liquid phase.

In this case, the gas-liquid separator 51 may be referred to as a mist separator, a heavy carbon separator, etc., and the liquid heavy carbon may be returned to the liquefied gas storage tank 10 or may be delivered to a separate 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. Although the forced vaporizer 50 heats the liquefied gas, the vaporized liquefied gas has a temperature (for example, -100 deg.) For allowing the heavy carbon to remain in the liquid phase, and therefore it may be lower than the temperature required by the customer 20 .

Thus, the heater 52 can heat the liquefied gas using a variety of heat sources, similar to the forced vaporizer 50, wherein the heat source can be shared with the forced vaporizer 50 and / or the vaporizer 42.

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

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

The forced vaporizer 50 vaporizes the liquefied gas to about -100 degrees, which is to remove the heavy carbon as described above. At this time, the forced vaporizer 50 is provided with a liquefied gas regulator (not shown) so that the state (temperature, etc.) of the liquefied gas delivered from the forced vaporizer 50 to the heavy carbon separator and / .

The gas supply portion in the present embodiment may further include an H / D compressor 36, a remelting device 37, and a return pump 38.

The H / D compressor 36 may be used for compressing the evaporated gas generated in the liquefied gas storage tank 10 during bunkering to discharge or incinerate it to the outside, and the type of the compressor is not limited.

The re-liquefier 37 can re-liquefy the surplus evaporated gas through the re-liquefied refrigerant and return it to the liquefied gas storage tank 10. The re-liquefier 37 may include a re-liquefier heat exchanger (not shown) and a re-liquefied refrigerant supply device (not shown).

The re-liquefier 37 supplies cold heat to re-liquefy the evaporated gas through the re-liquefied refrigerant supply device, and the refrigerant supplied from the re-liquefied refrigerant supply device is supplied to the re-liquefied heat exchanger through a separate pump (not shown) So that the evaporation gas can be supplied with cold heat for re-liquefaction.

The return pump 38 is connected to the gas-liquid separator 35 for separating the vaporized gas re-liquefied in the liquid remover 37 into a liquid phase and a gaseous phase and a liquid phase to the liquefied gas storage tank 10 through the tenth line L10 Can supply.

At this time, in the present invention, when the liquid phase is not supplied to the liquefied gas storage tank 10 in the gas-liquid separator 35 (the pressure difference between the gas-liquid separator 35 and the liquefied gas storage tank 10) Liquid separator 35 is supplied to the liquefied gas storage tank 10 through the eleventh line L11 and bypass valves (not shown), which are the bypass line, and the return pump 38 .

Liquid separator 35 is stored at a pressure higher than the internal pressure of the liquefied gas storage tank 10, it is supplied to the liquefied gas storage tank 10 through the tenth line L10 Liquid separator 35 is stored at a pressure lower than the internal pressure of the liquefied gas storage tank 10, the liquefied gas supply pump 38 is driven to supply the liquefied gas from the liquefied gas storage tank 10).

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

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

Hereinafter, the processing mechanism of the liquefied gas stored in the liquefied gas storage tank 10 and the processing mechanism of the evaporated gas generated in the liquefied gas storage tank 10 are described in detail.

First, the gas processing system 1 according to the embodiment of the present invention is constructed so that the liquefied gas stored in the liquefied gas storage tank 10 is supplied to the first line L1 And then the impurities of the liquefied gas are filtered through a strainer (not shown), and then a) the sixth line L6 is supplied to the customer 20 To the forced vaporizer 50 or b) 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 at least partially by the forced vaporizer 50 and the forcedly vaporized liquefied gas is supplied to the gas-liquid separator 51 The gas is separated into a gas and a liquid and the heavy carbon is separated into a liquid and returned to the liquefied gas storage tank 10 while 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 by the high pressure pump 41 to a high pressure and vaporized by the vaporizer 42 and then supplied to the high pressure consumer 21 .

The gas processing system 1 according to the embodiment of the present invention can be constructed such that the evaporation gas generated in the liquefied gas storage tank 10 is separated into c) the second evaporation gas generated in the liquefied gas storage tank 10, Line L2 or d) the third line L3 by using the evaporative gas compressor 30 so as to supply the compressed gas to the consumer 20.

c) The evaporation gas supplied through the second line (L2) can be multi-stage compressed at a high pressure by the evaporation gas compressor (30) and can be supplied to the high pressure consumer 21, and through the process of b) described above, They can also join with the vaporized liquefied gas and be supplied to the high-pressure consumer 21 together.

d) The evaporation gas supplied through the third line (L3) is an evaporation gas supplied from the second or third stage of the evaporation gas compressor (30) supplied with the evaporation gas supplied through the second line (L2) May be supplied to the low-pressure consumer 22 and may be supplied to the low-pressure consumer 22 by joining with the liquefied gas vaporized through the process of a) described above.

At this time, the forced vaporized liquefied gas supplied through the forced vaporizer 50 may be supplied when the fuel consumption amount of the low-pressure consumer 22 increases, but is not limited to this example. (The liquefied gas stored in the liquefied gas storage tank 10 is liquefied by using the forced vaporizer 50 and the gas-liquid separator 51 to lower the liquefied gas having a high proportion of the heavy carbon, So that the efficiency of the low-pressure consumer 22 can be increased.)

Of course, the evaporative gas generated in the liquefied gas storage tank 10 can be supplied to the gas-fired device 23 and the vent mast 24 as described above. In this case, a separate line (not shown) (Not shown) provided on the line to the gas-fired device 23 or to the vent mast 24.

The gas treatment system 1 according to the embodiment of the present invention may include a technique in which the liquefied gas storage tank 10 accumulates the evaporated gas therein.

The evaporation gas generated in the liquefied gas storage tank 10 of the embodiment of the present invention is supplied to the evaporation gas consuming station 20 when the internal pressure of the liquefied gas storage tank 10 is equal to or higher than the preset pressure, The pressure in the liquefied gas storage tank 10 is accumulated. Here, the preset pressure may be 1.06 bar to 1.12 bar, and the evaporation gas consuming place 20 may include a gas combustion device 23, a vent mast 24, and the internal pressure of the liquefied gas storage tank 10 may be In the case of less than the set pressure, it may be the case that the driving of the engine 20 causing the propulsion of the ship (not shown) is stopped, 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 lower than the preset pressure, the operation of the evaporative gas compressor 30 is stopped, and the evaporation gas generated in the liquefied gas storage tank 10 It is possible to pressurize the liquefied gas in the liquefied gas storage tank 10 as it is.

In the embodiment of the present invention, when the internal pressure of the liquefied gas storage tank 10 is equal to or higher than the preset pressure, more specifically, when the internal pressure of the liquefied gas storage tank 10 is 1.17 bar to 1.20 bar, The evaporation gas generated in the evaporator 10 is pressurized by the evaporation gas compressor 30 and supplied to the gas combustion apparatus 23 for burning the evaporation gas so that the internal pressure of the liquefied gas storage tank 10 is 1.20 bar to 1.25 bar The evaporated gas generated in the liquefied gas storage tank 10 is supplied to the vent mast and is discharged to the outside. When the internal pressure of the liquefied gas storage tank 10 is 1.25 bar or more, the liquefied gas storage tank 10 may be supplied to a safety valve (not shown) and may be discharged from the inside of the liquefied gas storage tank 10 to the outside through a safety valve.

As described above, in the embodiment of the present invention, it is necessary to operate the evaporative gas compressor (30) in order to discharge and discharge the evaporative gas to the outside by accumulating the evaporative gas generated in the liquefied gas storage tank (10) The power consumption can be reduced and the evaporation gas can be prevented from being discharged to the outside, so that waste of the evaporation gas can be prevented.

The gas treatment system 1 according to the embodiment of the present invention may include a technique for commonly using the H / D compressor 36 at the time of bunkering and maintenance of the liquefied gas storage tank 10.

The gas processing system 1 according to the embodiment of the present invention includes an H / D compressor 36 for pressurizing evaporative gas generated in the liquefied gas storage tank 10, an evaporator 36 for compressing the evaporated gas by the H / D compressor 36, (Not shown) for heating the gas and the evaporation gas generated in the liquefied gas storage tank 10 during the bunkering or onshore storage where the liquefied gas to be supplied to the liquefied gas storage tank 10 is stored And a temporary storage (not shown) as main components.

When the liquefied gas is first loaded from the outside to the liquefied gas storage tank 10 (including the case where the liquefied gas is shipped after completion of the maintenance work of the liquefied gas storage tank 10), that is, when bunkering, Is a very low temperature ignitable material, a special work, that is, a replacement operation other than a general storage tank, must be preceded.

Generally, the replacement method of the liquefied gas storage tank 10 is to supply the dry gas to the inside of the liquefied gas storage tank 10 to remove moisture, and to remove the inert gas from the liquefied gas storage tank 10 To remove oxygen. Thereafter, a cool-down process is performed in which the hydrocarbon gas is supplied to the interior of the liquefied gas storage tank 10 to remove the inert gas, and the liquefied gas storage tank 10 is cooled using the liquefied gas . When the cooldown process is completed, the replacement method is completed, and then the liquefied gas such as LNG is supplied to the inside of the liquefied gas storage tank 10 to perform the shipment work.

On the contrary, when unloading the liquefied gas stored in the liquefied gas storage tank 10 to the shore (including removing all of the liquefied gas before the maintenance work of the liquefied gas storage tank 10) , An operation slightly different from that described above is performed.

First, the liquefied gas stored in the liquefied gas storage tank 10 is discharged to the customer. At this time, the remaining liquefied gas is present, and a warm-up step is performed to remove all remaining liquefied gas. In the warming-up step, the evaporated gas generated in the liquefied gas storage tank 10 is compressed by a compressor and then heated by a separate heater to return to the liquefied gas storage tank 10, thereby increasing the internal temperature of the liquefied gas storage tank 10 So that the remaining liquefied gas is all vaporized. In order to remove all of the evaporation gas remaining in the liquefied gas storage tank 10 after the warm-up step, an inert gas is supplied, a drying gas is supplied to dry the inside, and oxygen is supplied to supply air therein. By the above process, the unloading process of the liquefied gas storage tank 10 is completed, and thereafter, the operator can perform the maintenance work or the like.

During the liquefied gas loading process (bunkering), even when the liquefied gas storage tank 10 cools down, many evaporative gases are generated at the time of loading the liquefied gas. At this time, the internal pressure of the liquefied gas storage tank 10 rises A compressor is used to discharge the generated evaporated gas to the outside (Shore).

Also, during the liquefied gas unloading process, the compressor is used in the process of compressing the evaporated gas in order to raise the internal temperature of the liquefied gas storage tank 10 in the warm up step.

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.

That is, the H / D compressor 36 pressurizes the evaporation gas generated during the bunkering to supply it to the shore consumer, or when the liquefied gas is unloaded (before the maintenance of the liquefied gas storage tank 10) The vaporized gas remaining in the liquefied gas storage tank 10 may be pressurized and returned to the liquefied gas storage tank 10 to circulate the vaporized gas to the liquefied gas storage tank 10.

Specifically, the H / D compressor 36 can supply the evaporative gas generated in the liquefied gas storage tank 10 through the seventh line L7 during bunkering to the shore, The evaporation gas remaining in the liquefied gas storage tank 10 is compressed by the heater 361 after the liquefied gas unloading (before maintenance of the liquefied gas storage tank 10) The refrigerant gas is returned to the liquefied gas storage tank 10 through the twelfth line L12 so that the evaporated gas is supplied to the liquefied gas storage tank 10, the H / D compressor 36, the heater 361, the liquefied gas storage tank 10, In order. Thus, 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 outside 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 compresses the evaporation gas generated during bunkering and discharges it to a shore consumer, and at the same time, when the liquefied gas is unloaded (the liquefied gas storage tank 10 is opened It is possible to increase the temperature of the remaining evaporating gas to vaporize all of the remaining liquefied gas stored in the liquefied gas storage tank 10 and to pressurize the liquefied gas storage tank 10 so as to be circulated.

As described above, in the embodiment of the present invention, since the H / D compressor 36 can be commonly used at the time of bunkering, liquefied gas unloading, or maintenance of the liquefied gas storage tank 10, , The space for building the system is reduced, thereby maximizing the use space in the ship.

The gas processing system 1 according to the embodiment of the present invention may further include a reducing valve 341 in addition to the re-liquefier 37 to improve the re-liquefaction rate, a return pump 35), and techniques for sharing the line through which the vaporized gas is supplied to the GCU 23 and the liquefaction unit 37. [

The gas processing system 1 according to the embodiment of the present invention includes an evaporative gas compressor 30 for multi-stage pressurizing the evaporative gas generated in the liquefied gas storage tank 10, an evaporative gas compressor 30 for condensing the evaporated gas compressed in the evaporative gas compressor 30 A first reducing valve 341 for reducing or expanding the evaporated gas compressed in the evaporating gas compressor 30; a second reducing valve 341 for reducing or at least partially liquefying the evaporated gas through the re-liquefying device; A gas-liquid separator 35 for separating the vaporized gas re-liquefied through the second pressure-reducing valve 342 and the second pressure-reducing valve 342 for expanding the gas into liquid and vapor, do.

The redistribution device 37 can liquefy the evaporated gas branched at the middle end of the evaporated gas compressor 30 and compressed at a low pressure (13 bar to 15 bar) through the refrigerant, and more specifically, The evaporated gas which is branched at the middle end of the evaporator 30 and compressed at a low pressure (13 bar to 15 bar) is firstly reduced from 7 bar to 8 bar through the first pressure reducing valve 341 and then cooled through the re-liquefier 37, The cooled evaporated gas may be secondarily reduced from 5 bar to 6 bar through the second pressure reducing valve 342.

As described above, the embodiment of the present invention further includes the pressure reducing valve 342 at the rear end of the liquefaction device 37 to further improve the liquefaction efficiency.

The gas-liquid separator 35 supplies the separated gas phase to the gas combustion device 23 consuming the flash gas via the heater 33, and the separated liquid phase is supplied to the liquefied gas storage tank 10 Can be returned. In the embodiment of the present invention, the return line L10 (tenth line) connecting the gas-liquid separator 35 and the liquefied gas storage tank 10, the bypass line L11 bypassed on the return line L10 11) and a pump 38 (return pump) provided on the bypass line L11 for returning the liquid liquefied gas stored in the gas-liquid separator 35 to the liquefied gas storage tank 10 and a first pressure reducing valve 341 And a branch line (not shown) that branches off between the liquefaction device 37 and the liquefaction device 37 and supplies the gas to the gas combustion device 23. [

More specifically, the liquid liquefied gas stored in the gas-liquid separator 35 is supplied to the liquefied gas storage tank 10 through the return line L10 (tenth line) when the internal pressure of the gas-liquid separator 35 is equal to or higher than the predetermined pressure value Liquid separator 35 is lower than the pre-set pressure value, it is possible to drive the return pump 38 to be supplied to the liquefied gas storage tank 10 through the bypass line L11 (eleventh line) have.

That is, since the gas-liquid separator 35 stores the evaporated gas that is secondarily reduced in pressure from 5 bar to 6 bar through the second pressure reducing valve 342, the decompressed evaporated gas in the liquid phase, which is larger than the internal pressure of the liquefied gas storage tank 10, Liquid separator 35 is supplied to the liquefied gas storage tank 10 through the return line L10 when the internal pressure of the gas-liquid separator 35 is equal to or higher than the preset pressure value, It is possible to prevent the driving power consumption of the liquefied gas storage tank 10 and to return to the liquefied gas storage tank 10 in a stable manner.

When the supply amount of the evaporation gas branched at the intermediate stage of the evaporation gas compressor 30 and compressed at the low pressure is larger than the preset supply amount, the branch line is branched at the intermediate stage of the evaporation gas compressor 30, When at least a part of the evaporation gas is supplied to the gas combustion device 23 and the supply amount of the evaporation gas compressed at the low pressure branching at the middle end of the evaporation gas compressor 30 is smaller than the predetermined supply amount, It is possible to supply all of the evaporated gas compressed at the low pressure to the liquefaction device 37 at the intermediate stage of the liquefier.

That is, the first pressure reducing valve 341 and the second pressure reducing valve 342 are provided on the fourth line L4 to provide a side stream line of the evaporating gas compressor 30 in addition to the fourth line L4 It is possible to minimize the number of branch lines of the evaporative gas compressor 301 and to improve the driving reliability of the system. (If the number of side stream lines of the evaporative gas compressor 30 increases, Falling)

Here, the preset pressure value is 5 bar to 6 bar, the remelting device 37 uses nitrogen as the refrigerant, and the second pressure reducing valve 342 can be a line-thrombose valve.

The gas processing 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 high pressure consumer 21, And the like.

The gas processing system 1 according to the embodiment of the present invention includes a boosting pump 40 for firstly pressurizing the liquefied gas stored in the liquefied gas storage tank 10, a liquefied gas which is primarily pressurized from the boosting pump 40 A high pressure pump 41 for supplying secondary pressurized gas to the high pressure pump 41 and a secondary pressurizing pump 42 for supplying secondary pressurized liquefied gas from the high pressure pump 41 to the vaporizer 42; A low pressure consumer 22 for supplying and consuming the evaporated gas branched at the intermediate stage of the evaporation gas compressor 30 and pressurized at a low pressure, A forced vaporizer 50 for supplying a liquefied gas stored in the forced vaporizer 50 to the forced vaporizer 50 and a low pressure consumer 22 for supplying the liquefied gas forcedly vaporized from the forced vaporizer 50, Liquid separator And a separator 51 as an essential component.

The boosting pump 40 first pressurizes the liquefied gas stored in the liquefied gas storage tank 10 and supplies it to the high pressure pump 41 or the forced vaporizer 50 so that the high pressure pump 41 And the use of a pump to supply the forced vaporizer 50.

Here, the forced vaporizer 50 supplies the liquefied gas stored in the liquefied gas storage tank 10 from the boosting pump 40 in a primary pressurized state to the low pressure consumer 22, It is possible to supply the fuel to the customer 22. Accordingly, the present embodiment has the effect of omitting the provision of the pressure reducing valve at the inlet end of the low-pressure consumer 22.

The forced vaporizer 50 is supplied with the liquefied gas stored in the liquefied gas storage tank 10 from the boosting pump 40 in a primary pressurized state and supplied to the front end of the evaporative gas compressor 30 after vaporizing . In this embodiment, since the demanded pressure of the consumer 20 is adjusted by the evaporative gas compressor 30, the delivery pressure of the boosting pump 40 can be lowered. Of course, the liquefied gas supplied to the forced vaporizer 50 can also be supplied through the booster pump 40 supplied with the liquefied gas by the high-pressure pump 41 in this case as well.

By sharing the use of the pump supplied to the high pressure pump 41 and the forced vaporizer 50 through the boosting pump 40 as described above, there is an effect that the construction cost of the pump 40 can be reduced, and the forced vaporizer 50 The pressure of the liquefied gas in the liquefied gas storage tank 10 is lowered and the driving power of the pump 40 is reduced.

The gas processing system 1 according to the embodiment of the present invention is provided with the return line L10 of the gas-liquid separator 35 provided at the rear stage of the liquefaction device 37, the cooldown circulation line L13 of the high- , And a return line (not shown) of the gas-liquid separator 51 provided at the rear end of the forced vaporizer 50, respectively.

The gas processing system 1 according to the embodiment of the present invention is provided with a remanufacturing device 37 for re-liquefying the evaporation gas compressed in the evaporation gas compressor 30, Liquid separator 35 for separating the liquefied gas into liquid and liquid, 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, A cool down circulation line L13 (line 13) connected to the liquefied gas storage tank 10 from the high-pressure pump 42 at the time of cooldown of the high-pressure pump 42, a gas-liquid separator 51 for separating the liquid- (10th line) of the gas-liquid separator 35 for returning the liquid phase of the gas-liquid separator 35 to the liquefied gas storage tank 10 and the return line And a return line (not shown) of the gas-liquid separator 51 as main components.

The line L13 returning from the high-pressure pump 41 to the liquefied gas storage tank 10 during the cool-down of the high-pressure pump 41, the liquid phase of the gas-liquid separator 35 to the liquefied gas storage tank 10, and a line returning the liquid phase of the gas-liquid separator 51 to the liquefied gas storage tank 10 may be shared.

Thus, by sharing at least one or more return lines 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, Thus, the reliability of the system can be improved, and the return can be stably realized. Also, since the return line is shared and cooldown can be preliminarily performed, the evaporated gas in the liquid phase returns to the liquefied gas storage tank 10, There is an effect that no recurrence occurs. That is, there is an effect that the substantial re-liquefaction efficiency is increased.

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

When the high pressure consumer 21 is driven through the liquefied gas and when the evaporative gas is simultaneously re-liquefied by the refill liquor 37, the discharge pressure of the gas-liquid separator 35, that is, 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 a back pressure is applied to the return line L10 to flow back to the gas-liquid separator 35.

However, in the embodiment of the present invention, the case where the high-pressure consumer 21 is driven through the liquefied gas and the case where the evaporated gas is re-liquefied by the liquefaction device 37 do not occur at the same time, 41 and the return line of the gas-liquid separator 35 so as to prevent backpressure from being applied on the shared line and to effectively share the return line. (Liquefaction device 37 is driven In this case, since the evaporation gas is supplied to the high-pressure consumer 21 through the evaporative gas compressor 30 in a sufficient amount, the liquefied gas can be supplied to the high-pressure consumer 21), so that the high-pressure pump 41 is not driven.

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

Since the forced vaporizer 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, The return line of the gas-liquid separator 51 and the cooldown circulation line L13 of the high-pressure pump 41 can be shared.

Therefore, the return line of the gas-liquid separator 51 is previously cooled by the cooldown 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 regenerated, It is possible to efficiently manage the internal pressure of the fuel cell stack 10. Of course, at this time, the return line of the gas-liquid separator 51 and the cooldown circulation line L13 of the high-pressure pump 41 differ from each other at the time when they flow to each other, 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 is a technique that simplifies the cooldown 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 .

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

The bypass line connecting the front end of the forced vaporizer 50 and the return line of the gas-liquid separator 51 is provided so that the bypass line of the forced vaporizer 50 and the return line of the gas-liquid separator 51 Lines can be shared together.

The bypass line of the forced vaporizer 50 is connected to the return line of the gas-liquid separator 51 other than the front end of the gas-liquid separator 51 so that the bypass function of the forced vaporizer 50 and the return line of the gas- It is possible to share the cooldown function, and the cooldown of the gas-liquid separator 51 is simplified and optimized.

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

Hereinafter, a description will be made with reference to FIGS. 2A to 2C. First, the first and second embodiments 42a and 42b of the vaporizer 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 gas treatment system 1 according to the embodiment of the present invention are provided with a vaporizer 424 for vaporizing the liquefied gas stored in the liquefied gas storage tank 10 through the vaporized vapor A first heat exchanger 4231 for supplying heat to the vaporized fruit and a second heat exchanger 4232 for supplying vaporized heat to the vaporized heat, And a circulation pump 422 for circulating the heat to supply the vapor to the vaporizer 424. [

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

Here, the first vaporizer feeder 4231 and the second vaporizer feeder 4232 are arranged such that the first vaporizer feeder 4231 is a plate type and the second vaporizer feeder 4232 is a shell & tube And the types of heat exchangers may be different from each other. Of course, two heat exchangers can be used in the same way as Plate type or Shell & Tube type. Further, the vaporizing second supply device 4232 can use steam or seawater as a heat source to be supplied to the vaporized fruit.

In the first and second embodiments 42a and 42b of the gas treatment system 1 according to the embodiment of the present invention, the front end and the rear end of the vaporized first supply device 4231 are connected to each other to supply the vaporized first supply A first bypass line GBL1 (vaporized first branch line) for vaporizing the vaporized fruit passing through the apparatus 4231 from the rear end of the vaporized first supply device 4231 to the front end thereof, a vaporized second supply device 4232 And a second bypass line GBL2 for bypassing the vaporized energy passing through the vaporizing second supply device 4232 from the rear end of the vaporizing second supply device 4232 to the front end, A control unit 902 for controlling the first bypass line GBL1 or the second bypass line GBL2 and a vaporization storage tank 421 for storing vaporized fruits.

The control unit 902 drives the vaporized first branch line GBL1 or the vaporized second branch line GBL2 to reheat vaporized beryllium if the vaporized fuel supplied to the vaporizer 424 is equal to or lower than the preset temperature value . Here, the preset temperature value is an image of 85 degrees to 95 degrees, and the vaporizing second supply device 4232 can be supplied with a heat source depending on the heat source supply capability of the vaporizing first supply device 4231.

In the first embodiment 42a of the gas treatment system according to an embodiment of the present invention, the vaporized fruit is heated / cooled circulated. The vaporized fruit stored in the vaporized fruit storage tank 421 is circulated through the vaporized fruit cycle (Jacket cooling water) by the vaporized first supply device 4231 and can be heated to a maximum image temperature of 70 degrees, and then the vaporized second supply device 4232 is heated by the vaporized first supply device 4231, (Preferably 90 degrees), and then is supplied to the vaporizing heat exchanger 424 and is supplied to the first line L1 through the first line L1 The liquefied gas at 130 degrees can be heated to an image 35 to 55 degrees, and the vaporized refrigerant can be cooled from the image 90 degrees to the image 50. [

Since the engine cooling water is supplied by the vaporizing first supply device 4231 and the amount of the engine cooling water is varied according to driving of the engine during heating, the amount of heat source supply of the engine cooling water may be reduced when the engine cooling water is driven at a low speed, (4232) can be varied depending on the vaporizing first supply device 4231 and can be heated. The control unit 902 may be configured to receive the temperature information of the liquefied gas or vaporized beryllium from the first temperature measurement device 921 and the second temperature measurement device 922 And it is possible to heat the vaporized berries by driving the first bypass line GBL1 or the second bypass line GBL2 according to the circumstances described above.

A description will be made of a process of heating / cooling circulation of the vaporized fruit in the second embodiment 42b of the vaporizer of the gas processing system 1 according to the embodiment of the present invention. Only the procedure of the evaporator 422 is changed. Therefore, it is the same as that described in the first embodiment 42a of the vaporizer described above.

Hereinafter, the third embodiment 42c of the vaporizer will be described.

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 processing system 1 according to the embodiment of the present invention is provided with the vaporization heat exchanger 424, the vaporized first supply device 4231, the vaporized second supply device 4232, A circulation pump 422, a heater 4233 (a vaporized additional heater) provided at a rear stage of the vaporized first supply device 4231 and further heating the vaporized heat heated in the vaporized first supply device 4231, A bypass line GBL4 provided at the rear end of the first supply device 4231 for supplying vaporized heat heated by the vaporizing first supply device 4231 to the front end of the vaporizing second supply device 4232, The third branch line).

The first vaporizer feeder 4231 and the second vaporizer feeder 4232 are arranged such that the first vaporizer feeder 4231 and the second vaporizer feeder 4232 are connected in parallel, The feeder 4231 first heats the vaporized fruit and the vaporized second feeder 4232 can heat the vaporized feeder lanes and the vaporized first feeder 4231 and the vaporized second feeder 4232 May be disposed at the rear end of the circulation pump 422. [

Specifically, when the temperature of the rear end of the vaporizing first supply device 4231 is equal to or lower than a preset temperature, the vaporized beryllium heated by the vaporizing first supply device 4231 is heated by the heater 4233 Or may be supplied to the upstream side of the vaporization second supply device 4232 via the bypass line GBL4.

The vaporizing first supply device 4231 is a plate type and the vaporizing second supply device 4232 is a Shell & Tube type. The two types of heat exchangers may be different. Of course, two heat exchangers may be plate type or shell & tube May be used in the same kind. The vaporizing second supply device 4232 can use steam or seawater as a heat source to be supplied to the vaporized fruit.

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

However, since the amount of engine cooling water varies depending on the driving of the engine, it is difficult to always supply a constant heat source to the evaporation heat exchanger 424 due to a severe temperature change. In order to prevent this, the present invention may further include a vaporized-material additional heater 4233. In the present invention, when the engine is driven at low speed and the supply amount of the heat source of the engine cooling water is reduced, the image can be heated up to 90 degrees by reheating through the additional heater 4233. The liquefied gas supplied to the vaporization heat exchanger 424 and flowing through the first line L1 may be heated to an image 35 to 55 degrees and the vaporized refrigerant may be cooled from the image 90 degrees to the image 50 .

Here, the vaporizing second supply device 4232 is variable depending on the vaporizing first supply device 4231 and can be heated. The control unit 902 may be configured to receive the temperature information of the liquefied gas or vaporized beryllium from the first temperature measurement device 921 and the second temperature measurement device 922 And it is possible to heat the vaporized berries by driving the first bypass line GBL1 or the second bypass line GBL2 according to the circumstances described above.

In addition, the second supply device 4232 for supplying vaporized fuel stops driving the engine for a long time, so that the supply of the engine cooling water becomes very small, so that when the heating amount is not sufficient even with the vaporized-energy additional heater 4233, And is supplied to the vaporizing material circulation line GL without being supplied to the branch line GBL3, the vaporized material can be heated up to 90 degrees in the image.

In the third embodiment 42c of the vaporizer according to the embodiment of the present invention, since the amount of engine cooling water varies depending on the driving of the engine, when the supply amount of the heat source of the engine cooling water decreases at low speed driving, To the vaporizer second feeder 4232 and can be heated to 90 degrees by the vaporizer second feeder 4232

As described above, since the flow rate of the steam is reduced by the engine cooling water through the heating technology of the vaporized fruit through the parallel or series connection of the vaporizing and supplying device as described above, the operation of the boiler is reduced and fuel consumption can be reduced. The driving reliability of the vaporizer 42 is improved.

The gas processing system 1 according to the embodiment of the present invention may include a technique of implementing the processing of the liquefied gas and the evaporated gas through parallel driving according to the internal pressure of the liquefied gas storage tank 10. [

The gas processing system 1 according to the embodiment of the present invention includes an evaporative gas compressor 30 provided in parallel and a liquefied gas processing device 30 for supplying liquefied gas stored in the liquefied gas storage tank 10 to a customer, A liquefaction device 37 for re-liquefying the evaporated gas compressed by the evaporation gas compressor 30, a liquefaction device 37 provided at the rear stage of the liquefaction device 37, A gas burner 23 for consuming evaporative gas, and a forced vaporizer 50 for forcibly vaporizing the liquefied gas stored in the liquefied gas storage tank 10 are connected to the main decompression valve 342 for decompressing or expanding the evaporated gas .

Here, the liquefied gas processing apparatuses 40, 41, and 42 include a boosting pump 40 for firstly pressurizing the liquefied gas stored in the liquefied gas storage tank 10, a liquefied gas pressurized from the boosting pump 40 And a vaporizer (42) for supplying and vaporizing the liquefied gas pressurized at a high pressure from the high pressure pump (41) and the evaporation gas compressor (30) A compressor (not shown) and a second evaporative 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 BOG amount in the liquefied gas storage tank 10 is 75 to 85% And the third set pressure is less than the first set pressure and greater than 1.06 bar and the fourth set pressure is less than the third set pressure and may be greater than 1.03 bar.

First, the first evaporative gas compressor is basically driven. When the internal pressure of the liquefied gas storage tank 10 is equal to or higher than the first predetermined pressure, the second evaporative gas compressor is further driven. When the internal pressure of the liquefied gas storage tank 10 is lower than the first predetermined pressure, (40, 41, 42).

The evaporated gas generated in the liquefied gas storage tank 10 can be supplied to the refueling device 37 or the gas combustion device 23 when the internal pressure of the liquefied gas storage tank 10 is equal to or higher than the second predetermined pressure The internal pressure of the liquefied gas storage tank 10 is equal to or higher than the second predetermined pressure and the liquefied gas processing devices 40, 41, and 42 can be further driven have.

If the internal pressure of the liquefied gas storage tank 10 is lower than the third predetermined pressure, the driving of the first evaporative gas compressor can be stopped. If the internal pressure of the liquefied gas storage tank 10 is lower than the fourth predetermined pressure , The liquefied gas stored in the liquefied gas storage tank 10 is forcedly vaporized through the forced vaporizer 50 and the forced vaporized liquefied gas is returned to the liquefied gas storage tank 10 so that the internal pressure of the liquefied gas storage tank 10 Can be increased.

In the embodiment of the present invention, a pressure measuring device (not shown) for measuring the internal pressure of the control unit (not shown) and the liquefied gas storage tank 10 and a fuel requirement measuring device The control unit may receive the information from the pressure measuring device and the fuel required amount measuring device by wire or wireless, and the control unit may control the internal pressure of the liquefied gas storage tank 10, The liquefied gas processing apparatuses 40, 41, and 42 and the evaporative gas compressor 30 can be controlled with respect to the fluctuation in accordance with the set pressure.

As described above, in the embodiment of the present invention, the evaporation gas compressor 30 and the liquefied gas processing apparatuses 40, 41, and 42 are driven in parallel to enable the driving of the customer 20 to be resiliently performed without supplying oil, The system construction cost can be reduced.

The gas processing system 1 according to the embodiment of the present invention realizes the processing of the liquefied gas, the evaporation gas and the oil through the parallel driving according to the flow of the internal pressure when the internal pressure of the liquefied gas storage tank 10 is low ≪ / RTI >

The gas treatment system 1 according to the embodiment of the present invention is provided with the evaporation gas compressor 30, the refueling device 37, the liquefied gas processing devices 40,41 and 42, the second pressure reducing valve 342, And an oil treatment device (not shown) for supplying the oil stored in the storage tank (not shown) to the customer 20.

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

The evaporative gas compressor 30 is basically driven at the first preset pressure and when the amount of evaporative gas generated in the liquefied gas storage tank 10 is larger than the amount of fuel required in the consumer 20, The liquefied gas processing units 40, 41 and 42 and the oil processing unit can be further operated when the amount of evaporated gas generated in the liquefied gas storage tank 10 is smaller than the fuel required amount of the demander 20 . Preferably, the liquefied gas processing apparatuses 40, 41, and 42 are operated first, and the oil treatment apparatus can be operated in a lane.

Here, the first preset pressure may be 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%, or may be 1.06 bar to 1.12 bar.

At this time, in the embodiment of the present invention, the control unit receives the information from the pressure measuring device and the fuel required amount measuring device by wire or wireless, and determines that the internal pressure of the liquefied gas storage tank 10 described above is fluctuated according to the first preset pressure It is possible to control the liquefied gas processing devices 40, 41, and 42, the evaporative gas compressor 30, and the oil treatment device.

As described above, in the embodiment of the present invention, the stability of fuel supply to the system can be satisfied by driving the evaporation gas compressor 30, the liquefied gas processing units 40, 41, and 42 and the oil treatment apparatus in parallel, Is improved.

The gas processing system 1 according to the embodiment of the present invention realizes the processing of the liquefied gas, the evaporation gas and the oil through the parallel driving according to the flow of the internal pressure when the internal pressure of the liquefied gas storage tank 10 is high ≪ / RTI >

The gas processing system 1 according to the embodiment of the present invention includes, as main components, an evaporative gas compressor 30 and a remelting device 37 which are provided in parallel. Here, the evaporative gas compressor 30 may be provided in parallel to be equipped with a first evaporative gas compressor (not shown) and a second evaporative gas compressor (not shown).

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

When the internal pressure of the liquefied gas storage tank 10 is equal to or higher than a preset pressure, the first evaporative gas compressor is operated to supply the gas to the customer 20, and the liquefied gas stored in the liquefied gas storage tank 10 When the evaporation gas amount is larger, the remelting device 37 may be further operated or the second evaporative gas compressor may be additionally operated. Preferably. The second evaporative gas compressor is first operated and supplied to the customer 20 to increase the ship speed and the liquefaction device 37 can be operated in a lane. At this time, the preset pressure may be 1.11 bar to 1.13 bar.

As described above, in the embodiment of the present invention, the evaporative gas compressor 30 is driven in parallel, and further the liquefaction device 37 is driven to efficiently process the evaporated gas continuously discharged from the liquefied gas storage tank 10, The internal pressure of the tank 10 can be stabilized.

In the embodiment of the present invention, the preheating source having a configuration for preheating the evaporation gas compressor (30) in front of the evaporating gas compressor (30) used for forming the room temperature is used as an optimal preheating source in the ship ≪ / RTI >

The details of the technique will be described with reference to FIGS. 3A to 3D.

3A to 3D are conceptual diagrams of a gas processing system according to an embodiment of the present invention.

In this embodiment, the evaporation gas compressor 30, the evaporation gas cooler 31, the BOG-BOG heat exchanger 32, the first pressure reducing valve 341, the second pressure reducing valve 342, A separator 35, a liquid remover 37, and a preheater 39 as main components. Here, all the stages of the evaporative gas compressor 30 may be configured for room temperature, and some of the evaporation gas compressor 30 may be configured for the cryogenic temperature. The high pressure consumer 21 may be the engine 21, for example.

Here, the preheater 39 preheats the evaporated gas supplied to the evaporative gas compressor 30. The preheater 39 heats the evaporation gas supplied to the evaporation gas compressor 30 so that the evaporation gas compressor 30 can be used at room temperature and the heating source of the preheater 39 can be variously applied have.

For example, the heat source of the preheater 39 is a steam source, which receives steam from the evaporated gas compressor 30 through the evaporator gas cooler 31, receives the heat source from the heated evaporator gas, Liquefied refrigerant (for example, N2) and the BOG-BOG heat exchanger 32, and the refrigerant is evaporated through the BOG-BOG heat exchanger 32, The evaporation gas heated by the evaporation gas pressurized at the high pressure in the gas compressor 30, the evaporation gas compressed at the first stage of the evaporation gas compressor 30, the cooling water of the engine (for example, Jacket Cooling Water (JCW ) May be used, and the heat sources may be used in combination or selectively. This can be derived through a combination of the respective configurations, and the configuration is not particularly limited.

The preheater 39 can also use the various heat sources sequentially. For example, the pre-heater 39 may pre-heat with steam, secondarily preheat with the heat of the carburetor 42, and preheat the engine coolant supplied from the engine 21 to third degree, 21 and can preheat the heat of the vaporizer 42 or the engine coolant supplied from the engine 21 to the lane.

Hereinafter, embodiments in which the various heat sources described above can be applied through the configuration of the pre-heater 39 will be described.

First, in the present embodiment, the refrigerant of the re-liquefier 37 is used as the heat source of the pre-heater 39. In this case, the re-liquefier 37 is connected to the pre- Is used.

The preheater 39 is provided with a re-liquefaction heat exchanger 39a in the fourth line L4 and a preheating exchanger 39b in the second line L2 so that the re-liquefaction heat exchanger 39a and the preheat exchanger 39b, The liquefied heat exchanger 39a can receive the re-liquefied refrigerant through the re-liquefied refrigerant circulation line NL, and the pre-heat exchanger 39b can cool the re-liquefied heat exchanger 39a.

The preheater 39 is connected to the preheater 39 through the re-liquefied refrigerant supplied with the heat source from the evaporated gas pressurized in the evaporative gas compressor 30 to convert the evaporated gas discharged from the liquefied gas storage tank 10 from the image 1 to the image 40 And can be supplied to the evaporative gas compressor (30).

This embodiment is only an example in which the refrigerant of the liquefaction device 37 is used as a preheating source. The refrigerant of the liquefaction device 37 may be used as the preheating source in accordance with the type of the liquefaction device 37 Various methods of using can be applied.

As described above, in the present embodiment, the heat source can be efficiently used by using the refrigerant of the re-liquefier 37 as the heat source of the pre-heater 39, and the evaporator gas compressor 30, Can be used for room temperature, and the system construction cost can be reduced.

Next, the case of using steam, seawater, cooling water of the engine, and the heating source of the vaporizer 42 as the heat source of the pre-heater 39 will be described in the present embodiment (see FIG. 3B).

The preheater 39 further includes a preheater inlet 391 and a preheater outlet 392 to which a heating source of steam, seawater, engine coolant or an evaporator 42 is supplied to the preheater inlet 391, It is possible to preheat the evaporation gas supplied to the evaporation gas compressor 30 and to prevent the evaporation gas from being preheated by the preheater 39 so that the steam, seawater, cooling water of the engine or the heating source of the evaporator 42 can be supplied to the preheater outlet 392 .

That is, the pre-heater 39 is supplied to the evaporative gas compressor 301 through a heat source of steam, a heat source of seawater, a heat source of the heat of the vaporizer 42, and a heat source of engine cooling water supplied from the engine 21 Evaporate gas can be preheated

In the present invention, the preheater 39, the preheater 39 and the evaporator 42 are connected to each other through preheating sources, steam is supplied through a boiler in the ship, and seawater is circulated through the refrigerant used for the ballast water in the ship or the evaporative gas cooler 31 The heat source of the fruit can be supplied through the vaporizer 42 and the cooling water of the engine 21 can be supplied through the customer 20 so that the energy can be used efficiently and the evaporation gas compressor 30 can be used at room temperature And the system construction cost can be reduced.

Next, the case where the evaporative gas cooler 31 itself is used as the pre-heater 39 in the present embodiment will be described (see FIG. 3C).

In the present embodiment, any one of the evaporative gas coolers 31 (preferably, the evaporative gas cooler 39 at the downstream end of the initial stage of the evaporative gas compressor 30) may be used as the pre-heater 39. For example, when the evaporative gas cooler 39 at the initial stage rear end of the evaporative gas compressor 30 is used as the preheater 39, the evaporative gas supplied to the evaporative gas compressor 30 is supplied to the And is heated and preheated from the evaporation gas discharged from the first stage of the evaporation gas compressor 30 after introduction into the evaporation gas cooler 39 at the first end of the first end of the evaporation gas compressor 30, Is supplied to the first stage of the evaporative gas compressor (30).

The position of the preheater 39 as an evaporation gas cooler described above is merely an example, and the evaporator gas cooler provided at the other end, such as the second end, or the third end, of the evaporative gas compressor 30 may also be the preheater 39.

As described above, the pre-heater 39 is used as any one of the evaporative gas coolers provided between the evaporative gas compressors 30 to cool the compressed evaporative gas, The evaporation gas compressor 30 can be used for room temperature, and the system construction cost can be reduced.

Next, the case where the BOG-BOG heat exchanger 39 or the heater 39 is used as the heat source of the pre-heater 39 will be described in this embodiment (see FIG.

In the present embodiment, only the BOG-BOG heat exchanger 39 may be used as the pre-heater 39. [ When the preheater 39 is used as the BOG-BOG heat exchanger 39, the evaporated gas introduced into the evaporated gas compressor 30 can be heated and heated by the evaporated gas discharged from the evaporated gas compressor 30, The preheated evaporated gas is supplied to the evaporative gas compressor (30) only.

That is, it may seem similar to the embodiment in which the evaporative gas cooler 39 is selected as the embodiment in this case and the preheater 39, but the difference is that the embodiment in this case is the evaporator The evaporated gas directly flows into the evaporative gas compressor 30 but in the embodiment in which the evaporative gas cooler 39 is selected by the preheater 39, the evaporated gas discharged from the liquefied gas storage tank 10 is directly supplied to the evaporative gas cooler 39 ).

In the present embodiment, the BOG-BOG heat exchanger 39 and the heater can be selectively used as the pre-heater 39.

Specifically, in this embodiment, when the BOG-BOG heat exchanger 39 is driven, the evaporated gas supplied from the liquefied gas storage tank 10 bypasses the heater 39 through the fifteenth line L15, The BOG-BOG heat exchanger 39 is supplied to the gas compressor 30 (in this case, the BOG-BOG heat exchanger 39 is used as the preheater 39) 10 may be bypassed to the BOG-BOG heat exchanger 39 via the fourteenth line L14 to be preheated by the heater 39 and then supplied to the evaporative gas compressor 30 , In this case, the heater 39 is used as the preheater 39)

Here, the evaporative gas compressor (30) may be composed of multiple stages, the front end may be an evaporative gas compressor for room temperature, and the rear end may be composed of a cryogenic evaporative gas compressor, and the heater (36) may be steam.

At this time, the heater 39 or the BOG-BOG heat exchanger 39 preheats the evaporated gas discharged from the liquefied gas storage tank 10 to a temperature within a range of image 1 to image 40 degrees and supplies it to the evaporative gas compressor 30 Can supply.

In addition, in the embodiment of the present invention, the cryogenic and normal-temperature evaporative gas compressors 30 may be provided in parallel and the cryogenic compressor or the room temperature compressor may be selectively used depending on whether the BOG-BOG heat exchanger 39 is driven have.

Specifically, in this embodiment, when the BOG-BOG heat exchanger 39 is driven, the evaporated gas supplied from the liquefied gas storage tank 10 is supplied to the evaporative gas compressor for room temperature 30, and the BOG- When the unit 39 is not driven, the evaporated gas supplied from the liquefied gas storage tank 10 may be supplied to the cryogenic evaporative gas compressor 30. Accordingly, the evaporative gas compressor 30 can be selectively used depending on whether the BOG-BOG heat exchanger 32 is used, so that the system can be flexibly driven, thereby improving driving reliability.

As described above, in this embodiment, since the inlet temperature of the evaporative gas compressor 30 is increased to allow the evaporative gas compressor 30 to be used at room temperature, the elasticity of selection of the evaporative gas compressor 30 is increased, And it is possible to selectively use various heat sources other than the use of the preheater 39, thereby increasing the reliability of the driving.

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

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

1: Gas treatment system 10: Liquefied gas storage tank
20: Demand Source 21: High Pressure Demand Source
22: Low pressure consumer 23: Gas burner (GCU)
24: Vent Mast 25: Safety Valve
30: Evaporative gas compressor 31: Evaporative gas cooler
32: BOG-BOG heat exchanger 33: heater
341: first pressure reducing valve 342: second pressure reducing valve
35: gas-liquid separator 36: H / D compressor
361: Heater 37: Remelting device
38: return pump 39: preheater
39a: Re-liquefier heat exchanger 39b: Preheat exchanger
391: Preheating source inlet 392: Preheating source outlet
40: boosting pump 41: high pressure pump
42: vaporizer 421: vaporizer storage tank
422: Vaporization circulation pump 423: Vaporization feeder
4231: vaporized fruit first feeder 4232: vaporized fruit second feeder
4233: additional vaporizer heaters 424: vaporization heat exchanger
50: forced vaporizer 51: gas-liquid separator
52: heater 902:
921: first temperature measuring device 922: second temperature measuring device
L1 to L15: first to fifteenth lines GL: vaporized fruit circulation line
GLb: vaporized fruit branch line GBL1: vaporized fruit first branch line
GBL2: Second line of vaporized fruit line GBL3: Third line of vaporized fruit line
GBL4: vaporized fruit fourth quarter line NL: re-liquefied refrigerant circulation line

Claims (10)

An evaporative gas compressor for multiplying the evaporation gas generated in the liquefied gas storage tank by the multi-stage pressure and supplying the evaporation gas at room temperature;
A BOG-BOG heat exchanger for exchanging heat between the evaporated gas compressed by the evaporative gas compressor and the evaporated gas supplied from the liquefied gas storage tank; And
And a heater for further heating the evaporation gas supplied from the liquefied gas storage tank heated by the BOG-BOG heat exchanger,
When the BOG-BOG heat exchanger is not operated, the evaporated gas supplied from the liquefied gas storage tank bypasses the BOG-BOG heat exchanger, is preheated by the heater, and then supplied to the evaporative gas compressor.
When the BOG-BOG heat exchanger is driven,
The evaporation gas supplied from the liquefied gas storage tank is supplied to the evaporator
Wherein the gas is supplied to the evaporative gas compressor bypassing the heater or is first preheated in the BOG-BOG heat exchanger and secondarily preheated in the heater. delete delete The compressor according to claim 1,
Wherein the gas processing system comprises a multi-stage evaporative gas compressor for room temperature. The BOG-BOG heat exchanger according to claim 1,
Wherein the low-pressure evaporation gas is re-liquefied by supplying the evaporation gas compressed at a low pressure at the intermediate stage of the evaporation gas compressor. 6. The method of claim 5,
The evaporative gas compressor is composed of five stages,
Wherein the BOG-BOG heat exchanger branches off between the second and third stages of the evaporative gas compressor and supplies the evaporated gas compressed at a low pressure to re-liquefy the low-pressure evaporated gas. The method according to claim 1,
An evaporative gas decompressor for decompressing or expanding the evaporated gas compressed in the evaporative gas compressor; And
Further comprising a gas-liquid separator for separating the re-liquefied evaporated gas into vapor or liquid via the evaporative gas decompressor. The BOG-BOG heat exchanger according to claim 7,
Wherein the evaporation gas is supplied from the downstream end of the evaporation gas compressor to the high pressure evaporation gas at a high pressure and re-liquefies the high pressure evaporation gas. The BOG-BOG heat exchanger according to claim 1,
Characterized in that the evaporation gas compressed in the evaporation gas compressor is heat-exchanged with the evaporation gas supplied from the liquefied gas storage tank without liquefying a separate re-liquefying device. The BOG-BOG heat exchanger according to claim 1, wherein the heater or the BOG-
Wherein the evaporation gas discharged from the liquefied gas storage tank is preheated to a temperature within a range of 1 degree to 40 degrees and supplied to the evaporative gas compressor.

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