JP2018518415A - Ship including gas treatment system - Google Patents

Abstract

The ship including the gas processing system according to the present invention is characterized in that the evaporated gas reliquefied by the reliquefaction device is returned to the liquefied gas storage tank by the recovery line used when the pump is cooled down.

Description

  The present invention relates to a ship including a gas processing system.

  A ship is a means of transportation that sails through the ocean with a large amount of minerals, crude oil, natural gas, or thousands of containers, etc., made of steel, in a state of floating on the waterline surface by buoyancy, It moves with the thrust generated by the rotation of the propeller.

  Such a ship generates thrust by driving the engine. At this time, the engine moves the piston using gasoline or diesel, and rotates the crankshaft by the reciprocating motion of the piston. In general, the connected shaft rotates to drive the propeller.

  However, recently, an LNG fuel supply system for driving an engine using LNG as a fuel is used in an LNG carrier that transports liquefied natural gas (Liquid Natural Gas). In this way, LNG is used as engine fuel. The method used is also applied to ships other than LNG carriers.

  In general, LNG is known to be clean energy and richer in reserves than oil, and its usage is increasing rapidly as mining and transport technology develops. Such LNG is generally stored in a liquid state by lowering the temperature of methane, which is a main component, to −162 ° C. or less under 1 atm. The volume of liquefied methane is a gas in a standard state. It is about 1/600 of the methane volume in the state, and the specific gravity is 0.42, which is about one half of the crude oil specific gravity.

  However, the temperature, pressure, and the like necessary for driving the demand destination may differ from the state of the LNG stored in the tank. Therefore, recently, research and development on technology for controlling the temperature and pressure of LNG stored in a liquid state and supplying it to a demand destination has been continuously carried out.

  In addition, when LNG is stored in a liquid state, heat osmosis occurs in the tank, and a part of the LNG is vaporized to generate evaporative gas (BOG: Boil off Gas). In order to eliminate the risk of damage to the tank, the evaporative gas was simply discharged outside. However, recently, there is an increasing need for development of utilization methods such as re-liquefying the evaporative gas generated in the tank and supplying it to customers.

  The present invention was created to solve the above-described problems of the prior art, and the object of the present invention is to effectively supply liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer. It is to provide a ship including a gas processing system to supply.

  A ship including a gas processing system according to an embodiment of the present invention includes an evaporative gas supply line for connecting a liquefied gas storage tank and a high pressure gas injection engine, and a liquefaction for connecting the liquefied gas storage tank and the high pressure gas injection engine. A gas supply line, a pump provided on the liquefied gas supply line, pressurizing the liquefied gas stored in the liquefied gas storage tank and supplying the pressurized gas to the high pressure gas injection engine, and evaporation not supplied to the high pressure gas injection engine A reliquefaction device for reliquefying at least a part of the gas, a recovery line that is branched on the liquefied gas supply line and connected to the liquefied gas storage tank, and is used when the pump is cooled down, The evaporative gas liquefied by the reliquefaction device returns to the liquefied gas storage tank via the recovery line. The features.

  Specifically, the liquefied gas forcedly vaporized by the first gas-liquid separator that separates the evaporated gas reliquefied by the reliquefaction apparatus into gas and liquid and the forced vaporizer that forcibly vaporizes the liquefied gas is gasified. And a second gas-liquid separator that separates into liquid form, a first return line that returns the liquid separated by the first gas-liquid separator to the liquefied gas storage tank, and the second gas-liquid separator. A second return line for returning the liquid state to the liquefied gas storage tank, wherein at least a part of at least one of the first return line, the second return line, or the recovery line is shared with each other. Also good.

  Specifically, the pump may be a high-pressure pump that pressurizes to 200 bar to 400 bar.

  Specifically, a bypass line that connects the second return line may be further included in the previous stage of the forced vaporizer.

  Specifically, it may further include a heterogeneous fuel power generation engine that consumes the liquefied gas or the evaporated gas stored in the liquefied gas storage tank.

  Specifically, the first gas-liquid separator supplies the separated gas to a gas combustion device that consumes flash gas or evaporative gas, and the separated liquid is returned to the liquefied gas storage tank, In the two-gas / liquid separator, the separated gas may be supplied to the heterogeneous fuel power generation engine, and the separated liquid may be returned to the liquefied gas storage tank.

  Specifically, the liquefied gas flowing inside each of the first return line and the second return line merges with each other when the high pressure gas injection engine and the heterogeneous fuel power generation engine are all driven. You may return to a liquefied gas storage tank.

  Specifically, the second gas-liquid separator may be a heavy carbon separator that matches the methane number required by the heterogeneous fuel power generation engine.

  Specifically, a recovery pump provided on the first return line for returning the liquid liquefied gas stored in the first gas-liquid separator to the liquefied gas storage tank, and a detour for bypassing the recovery pump A liquid liquefied gas stored in the first gas-liquid separator, when the internal pressure of the first gas-liquid separator is equal to or higher than a preset pressure value, When the internal pressure of the first gas-liquid separator is less than a preset pressure value, it is supplied to the liquefied gas storage tank via the recovery pump, bypassing the recovery pump and supplied to the liquefied gas storage tank. May be.

  Specifically, the preset pressure value may be 5 bar to 6 bar.

  A ship including a gas processing system according to the present invention can effectively supply liquefied gas and / or evaporative gas from a liquefied gas storage tank to a customer, thereby improving the stability and reliability of the system.

It is a conceptual diagram of the gas processing system by one Example of this invention. It is a conceptual diagram of the vaporization system in the gas processing system of this invention. It is a conceptual diagram of the vaporization system in the gas processing system of this invention. It is a conceptual diagram of the vaporization system in the gas processing system of this invention.

  Objects, specific advantages and novel features of the invention will become more apparent from the following detailed description and preferred embodiments when taken in conjunction with the accompanying drawings. In this specification, it should be noted that, in the drawings, the same reference numerals are given to the components of the respective drawings, even if the same components are displayed on other drawings. is there. Further, in the description of the present invention, when it is determined that a specific description of a related known technique unnecessarily obscure the gist of the present invention, a detailed description thereof will be omitted.

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

  Hereinafter, the liquefied gas may be LPG, LNG, ethane, or the like, and can illustratively mean LNG (Liquid Natural Gas), and the evaporated gas is BOG (Boil Off Gas), which is naturally vaporized LNG or the like. Can mean.

  The liquefied gas may be referred to regardless of the state change such as a liquid state, a gas state, a mixed state of liquid and gas, a supercooled state, a supercritical state, and the like, and it is obvious that the evaporated gas is the same. In the present invention, the object to be processed is not limited to the liquefied gas, and may be a liquefied gas processing system and / or an evaporative gas processing system.

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

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

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

  The embodiment of the present invention may further include first to thirteenth lines L1 to L13. Each line may be provided with a valve (not shown) whose opening degree can be adjusted, and by controlling the opening degree of each valve, the supply amount of evaporative gas and / or liquefied gas and / or various refrigerants is controlled. Also good.

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

  The liquefied gas storage tank 10 may include a liquid liquefied gas and a gaseous evaporative gas. This is because evaporative gas can be generated when external heat penetrates into the liquefied gas storage tank 10 and the liquefied gas is heated.

  At this time, the evaporative gas causes an increase in the internal pressure of the liquefied gas storage tank 10 as the flow rate increases. Therefore, in order to protect the liquefied gas storage tank 10, it is desirable to discharge the evaporated gas. Therefore, according to the present invention, the evaporated gas can be appropriately discharged according to the pressure of the liquefied gas storage tank 10.

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

  Alternatively, the evaporative gas discharged from the liquefied gas storage tank 10 is cooled to a boiling point or lower by a reliquefaction device 37 or the like, which will be described later, and liquefied from a gaseous state to a liquid state (the liquefied evaporative gas and (Same / similar) may be processed such as returning to the liquefied gas storage tank 10.

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

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

  The heat insulating part insulates the inside and the outside of the liquefied gas storage tank 10 using a heat insulating material. The heat insulating part forms a heat insulating structure using various heat insulating materials such as polyurethane foam (PUF), pearlite (perlite), and wood (wood), and includes metals such as stainless steel (SUS) and invar (INVAR). Also good.

  When the liquefied gas storage tank 10 is a membrane type, the heat insulating part is marked with Mark III, No. The structure may be determined according to a conventionally well-known type such as 96, and when the liquefied gas storage tank 10 is an independent type, the structure is determined according to a conventionally well-known type such as MOSS or SPB. May be. 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 can form an empty space, and the empty space of the barrier portion is 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. May be.

  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 device provided outside. At this time, a nitrogen generator (N2 generator) may be used as the inert gas supply device.

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

  For example, the customer 20 is a low-pressure customer using liquefied gas having a pressure of about 1 bar to 10 bar (absolute pressure) such as a turbine low-pressure engine (DFDE, DFDG, XDF, etc.), a reliquefaction device, a boiler, a gas combustion device, or the like. Or a high pressure customer using a liquefied gas having a pressure of about 200 bar to 400 bar (absolute pressure) such as a high pressure engine (such as a ME-GI engine). It may be different.

  That is, in the present invention, the demand destination 20 comprehensively means all configurations that consume liquefied gas and the like, and in the present invention, the demand destination 20 is not limited to a specific configuration.

  The embodiment of the present invention has a configuration of a gas supply unit that processes liquefied gas or evaporated gas stored in the liquefied gas storage tank 10. Here, the gas supply unit is a configuration for transmitting liquefied gas and / or evaporative gas to the customer 20 through the engine and the like, and includes an evaporative gas compressor 30, a boosting pump 40, a high-pressure pump 41, and a vaporizer 42. Etc. may be included.

  The evaporative gas compressor 30 compresses the evaporative gas discharged from the liquefied gas storage tank 10. The evaporative gas compressor 30 may be a centrifugal type, a reciprocating type, or the like, and a plurality of the 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 unit may be provided such that all are centrifugal types, all are reciprocating types, or both a centrifugal type and a reciprocating type are mixed.

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

  For example, the evaporative gas compressor 30 in the present invention is a centrifugal type, and may be composed of two stages, three stages, five stages, six stages, and the like. Each stage number is simply compressed according to the requirement of the evaporative gas supplied according to the type of the customer 20, and does not mean that the larger the stage number, the higher the discharge pressure.

  Further, the evaporative gas compressor 30 may comprise a cryogenic compressor in order to process the evaporative gas in a low temperature state of about −100 degrees discharged from the liquefied gas storage tank 10. However, when the evaporative gas is compressed by the evaporative gas compressor 30, the temperature of the evaporative gas may rise. Therefore, some of the evaporative gas upstream of the multistage evaporative gas compressor included in the evaporative gas compression unit. The compressor may be a cryogenic compressor, and the remaining evaporative gas compressor downstream may be a room temperature compressor.

  When the temperature of the evaporation gas rises while the evaporation gas is compressed by the evaporation gas compressor 30, the volume of the evaporation gas may increase as the volume of the evaporation gas increases. This may cause an unnecessary load increase of the evaporative gas compressor 30, so that it is upstream of at least one evaporative gas compressor 30 and / or downstream of at least one evaporative gas compressor 30. An evaporative gas cooler (not shown) for cooling the compressed evaporative gas may be provided.

  The evaporative gas cooler can cool the evaporative gas using various cold heat sources. For example, the evaporative gas cooler can be seawater, a reliquefied refrigerant of the reliquefaction device 37, a liquefied gas, an evaporative gas, and a flash gas. Etc. may be used in various ways.

  In addition to the evaporative gas cooler, a buffer tank (not shown) may be provided between the stages of the evaporative gas compressor 30. The buffer tank may be provided to maintain a constant supply and supply pressure of the evaporative gas flowing into each stage of the evaporative gas compressor 30.

  The evaporative gas flowing into the evaporative gas compressor 30 may exchange heat with the compressed evaporative gas. However, since the evaporative gas flowing into the evaporative gas compressor 30 by heat exchange may be preheated, all of the evaporative gas compressor 30 may be composed of a normal temperature compressor.

  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 evaporative gas compressed by the evaporative gas compressor 30 is used for a low-pressure customer 22 such as a turbine, a low-pressure engine (DFDE, DFDG, XDF, etc.), a reliquefaction device, a boiler, a gas combustion device, etc., it is compressed. The pressure of the evaporated gas may be about 1 bar to 10 bar (absolute pressure), and when the compressed evaporated gas is used for a high pressure customer 21 such as a high pressure engine (such as ME-GI), the compressed evaporation The pressure of the gas may be about 200 bar to 400 bar (absolute pressure).

  Of course, the evaporative gas compressor 30 is provided in multiple stages, and the evaporative gas compressed to a low pressure by a part of the evaporative gas compressor 30 is discharged to the outside of the evaporative gas compressor 30 and used for the low-pressure customer 22. Alternatively, the evaporative gas further compressed to a high pressure by the remaining evaporative gas compressor 30 may be discharged outside the evaporative gas compressor 30 and used for the high-pressure customer 21.

  That is, in the evaporative gas compression unit having the evaporative gas compressors 30 provided in multiple stages, the pressure of the evaporative gas supplied to each customer 20, the number of evaporative gas compressors 30, the degree of multistage evaporative gas compression, etc. are particularly limited. It may not be decided variously.

  In order to transmit evaporative gas from the liquefied gas storage tank 10 through the evaporative gas compressor 30 to the low-pressure demand destination 22 or the high-pressure demand destination 21, the supply lines (second, third, 5, 7, 8 lines L2, L3, L5, L7, L8, etc.) may be provided.

  At this time, the supply line connected to the low pressure demand destination 22 in the evaporative gas compressor (end stage or intermediate stage) may be the low pressure supply line (third line L3), or the evaporative gas compressor 30 (end stage). The supply line connected to the high-pressure demand destination 21 in a stage or an intermediate stage may be a high-pressure supply line (second line L2). Therefore, the supply line may be branched into a low pressure supply line (third line L3) and a high pressure supply line (second line L2) with the evaporative gas compressor 30 as a reference.

  When the evaporative gas compressor 30 passes only a part of the evaporative gas compressor 30 provided in multiple stages, the evaporative gas is compressed to a low pressure and supplied to the low-pressure customer 22 along the low-pressure supply line L3, and provided in multiple stages. After passing through all of the evaporative gas compressor 30, the evaporative gas can be compressed to a high pressure and supplied to the high-pressure customer 21 along the high-pressure supply line L2.

  A part of the evaporative gas compressor 30 may not use lubricating oil, and the rest may use lubricating oil. For example, when 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 mixed into the evaporative gas), and the fourth to fifth stages are lubricated. Oil may be used (lubricating oil is mixed into the evaporative gas). This is because, in the case of the high pressure stage, the lubricating oil is required to smoothly drive the piston of the evaporative gas compressor 30 by changing the pressure of the evaporative gas to a high pressure.

  Of course, the number of the evaporative gas compressors 30 is not limited to the above. Among the plurality of evaporative gas compressors 30, a part of the former stage (low pressure stage) does not use lubricating oil, and the remaining part (high pressure stage) is lubricated. Oil may be used.

  The first pressure reducing valve 341 can depressurize or expand the evaporative gas pressurized by the evaporative gas compressor 30 and supplied to the reliquefaction device 37. Although not shown here, the first pressure reducing valve 341 decompresses or expands the evaporated gas pressurized by the evaporated gas compressor 30 and supplies it not only to the reliquefaction device 37 but also to the gas combustion device 23 and the like. can do.

  The first pressure reducing valve 341 is provided together with the second pressure reducing valve 342, and can evaporate or expand the evaporative gas pressurized by the evaporative gas compressor 30 in multiple stages. For example, the first pressure reducing valve 341 performs primary pressure reduction or primary expansion of the evaporative gas pressurized by the evaporative gas compressor 30 or the evaporative gas branched and supplied to the intermediate stage of the evaporative gas compressor 30. The evaporated gas supplied to the reliquefaction device 37 and subjected to heat exchange in the reliquefaction device 37 may be secondarily decompressed or expanded again by the second pressure reducing valve 342 and reliquefied.

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

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

  Here, the evaporative gas supplied to the gas-liquid separator 35 may be in a state of being cooled by being depressurized by the first pressure reducing valve 341 or the second pressure reducing valve 342. For example, the evaporative gas may be multi-stage pressurized in the evaporative gas compressor 30 to have a pressure of 200 bar to 400 bar, and the temperature may be around 45 degrees. The evaporative gas that has risen to a temperature of about 45 degrees is recovered by the reliquefaction device 37 via the first pressure reducing valve 341, and the evaporative gas heat-exchanged by the reliquefaction device 37 is also 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 evaporated gas is cooled by the reduced pressure, and may have a pressure of about 1 bar and a temperature of about −162.3 degrees.

  Thus, in the present embodiment, the evaporated gas supplied to the gas-liquid separator 35 is decompressed (or multistage decompressed) by the first decompression valve 341 or the second decompression valve 342 so as to have a temperature lower than −162 degrees. Therefore, about 30 to 40% of the evaporated gas can be liquefied. Thereafter, the gas-liquid separator 35 causes the liquefied gas to be collected in the liquefied gas storage tank 10 and supplied to the gas combustion device 232 via the ninth line L9 without throwing away the flash gas generated in the gas-liquid separator 35. Can be burned.

  The second pressure reducing valve 342 depressurizes or expands the evaporative gas pressurized by the evaporative gas compressor 30 and heat-exchanged by the reliquefaction device 37 to liquefy at least a part thereof. For example, the second pressure reducing valve 342 can reduce the evaporation gas to 1 bar to 10 bar, and when the evaporation gas is liquefied and transported to the liquefied gas storage tank 10, it can be reduced to 1 bar. The evaporative gas can also have a cooling effect.

  Here, the evaporative gas pressurized by the evaporative gas compressor 30 is cooled by exchanging heat with the evaporative gas supplied from the liquefied gas storage tank 10 in the reliquefaction device 37, but the pressure is the evaporative gas compressor 30. The discharge pressure discharged from can be maintained. In this embodiment, the evaporation gas can be liquefied by reducing the evaporation gas by using the second pressure reducing valve 342 so that the evaporation gas is cooled. At this time, as the pressure range to be depressurized is larger, the cooling effect of the evaporative gas can be increased. For example, the second pressure reducing valve 342 reduces the evaporative gas pressurized to 300 bar by the evaporative gas compressor 30 to 1 bar. The pressure can be reduced.

  The second pressure reducing valve 342 may be a Joule Thomson valve. Unlike this, the second pressure reducing valve 342 may comprise an expander (not shown). In the case of the Joule-Thomson valve, the evaporated gas can be effectively cooled by the reduced pressure, and at least a part of the evaporated gas can be liquefied. At this time, the expander may include an expander (not shown).

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

  Such a second pressure reducing valve 342, together with the first pressure reducing valve 341 described above, multi-stages the evaporative gas pressurized by the evaporative gas compressor 30 and heat-exchanged by the reliquefaction device 37, or evaporative gas compressor The evaporative gas branched and supplied to 30 intermediate stages can be depressurized in multiple stages, and this can be flexibly applied by changing the configuration according to each embodiment.

  The boosting pump (Boosting Pump) 40 and the high pressure pump (High Pressure Pump) 41 can pressurize the liquefied gas up to or near the pressure required by the customer 20. In the present invention, the demand destination 20 may be the high-pressure demand destination 21 and the low-pressure demand destination 22 or the like. However, since the pressure of the liquefied gas required for each demand destination 20 may be different, the boosting pump 40 as described above. And the high-pressure pump 41, or the boosting pump 40 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 may be variously determined from 10 bar to 400 bar (absolute pressure) according to the required pressure of the customer 20, and the present invention is not particularly limited thereto.

  At this time, a plurality of boosting pumps 40 and a plurality of high-pressure pumps 41 may be provided, and any one pump may be used as a main, and the other pump may be used as a backup. Needless to say, two or more pumps can be driven simultaneously to reduce the load.

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

  The lines L1 and L6 for supplying the liquefied gas may be a high-pressure liquefied gas supply line (first line) L1 connected from the liquefied gas storage tank 10 via the pumps 40 and 41 to the high-pressure customer 21 and / or Alternatively, the low-pressure liquefied gas supply line (sixth line) L6 connected to the low-pressure customer 22 from the liquefied gas storage tank 10 via the pump 40 may be used. When the high-pressure liquefied gas supply line L1 and the low-pressure liquefied gas supply line L6 are provided simultaneously, the high-pressure liquefied gas supply line L1 and the low-pressure liquefied gas supply line L6 may be branched from one liquefied gas supply line. Various determinations may be made 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 an extremely low temperature of about -160 degrees, but the required temperature of the liquefied gas required by the customer 20 is 10 to 50 degrees (preferably about 45 degrees). Can do. Therefore, when the liquefied gas is transmitted to the customer 20, the temperature rise of the liquefied gas is required.

  Of course, when the pressure of the liquefied gas is increased by the pumps 40 and 41, the temperature of the liquefied gas may rise. However, this is not sufficient, so the vaporizer 42 uses another heat source (steam, glycol water, seawater). The engine exhaust, engine coolant, electricity, etc.) can be used for heating.

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

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

  The vaporization heat medium circulation pump 422 is configured to supply the vaporization heat medium from the vaporization heat medium storage tank 421 to the vaporization heat exchanger 424. A plurality of vaporization heat medium circulation pumps 422 may be provided and connected in parallel or in series. In the case of gas, a heat source compressor (not shown) may be provided instead of the vaporization heat medium circulation pump 422.

  The vaporization heat medium supply device 423 heats the vaporization heat medium. Since the vaporized heat medium can be cooled while heating the liquefied gas in the vaporization heat exchanger 424, it is necessary to supplement the cooled vaporized heat medium with heat. Therefore, the vaporized heat medium can be heated by the vapor or the like, and then the liquefied gas can be heated by the vaporization heat exchanger 424.

  The vaporization heat medium supply device 423 includes a first vaporization heat medium supply device 4231 and a second vaporization heat medium supply device 4232, and a plurality of vaporization heat medium supply devices 423 may be provided. Here, the first supply device 4231 for vaporization heat medium and the second supply device 4232 for vaporization heat medium may be engine cooling water or seawater, and are configured in parallel or in series with each other. Also good.

  At this time, the vaporized heat medium flows along a vaporized heat medium circulation line GL that circulates and connects the vaporized heat exchanger 424, the vaporized heat medium supply device 423, the vaporized heat medium circulation pump 422, and the vaporized heat medium storage tank 421. be able to. However, the order of the components (vaporization heat exchanger 424, vaporization heat medium supply device 423, vaporization heat medium circulation pump 422, and vaporization heat medium storage tank 421) connected by the vaporization heat medium circulation line GL is different from the drawing. It may vary.

  The vaporization heat medium circulation line GL has vaporization heat medium branch lines GLb, GBL1 so that the vaporization heat medium supply device 423 can be bypassed and the temperature of the vaporization heat medium supplied to the vaporization heat exchanger 424 can be appropriately adjusted. GBL2 may be connected, and the vaporization heat medium branch lines GLb, GBL1, and GBL2 are branched from the vaporization heat medium circulation line GL upstream of the vaporization heat medium supply apparatus 423 and vaporized downstream of the vaporization heat medium supply apparatus 423. The heat medium circulation line GL may be merged.

  The vaporization heat exchanger 424 can vaporize the liquefied gas by supplying a heat source to the liquefied gas flowing on the liquefied gas supply line L1 through the circulating vaporized heat medium. The configuration type of the vaporization heat exchanger 424 may adopt various configurations of other heat exchangers such as shell & tube, and is not particularly limited.

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

  The low-pressure liquefied gas supply configuration may be provided together with the high-pressure liquefied gas supply configuration or independently, and this is not particularly limited because it may vary depending on the configuration of the customer 20.

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

  The forced vaporizer 50 vaporizes the liquefied gas. The forced vaporizer 50 receives the transmission of the liquefied gas from the liquefied gas storage tank 10 and / or the boosting pump 40, can be heated and vaporized using a heat source, and the heat source used at this time is the vaporizer 42. Steam, glycol water, seawater, engine exhaust, engine cooling water, electricity, and the like as described above may be used. The forced vaporizer 50 can also share a heat source with the vaporizer 42.

  The forced vaporizer 50 may be connected to the low-pressure liquefied gas supply line L6, and can vaporize the liquefied gas and transmit it to the low-pressure customer 22. At this time, methane, propane, butane, and the like are mixed in the liquefied gas. However, in the liquefied gas heated by the forced vaporizer 50, methane is vaporized, and propane, butane, and the like (hereinafter referred to as heavy carbon). A liquid state can be maintained.

  The gas-liquid separator 51 (or may be a heavy carbon separator) separates heavy carbon remaining in a liquid state with the vaporized liquefied gas. When a large amount of heavy carbon is flowed into the customer 20 (preferably the low-pressure customer 22) that consumes the liquefied gas, the driving efficiency may be lowered. Therefore, the present invention can increase the drive efficiency of the customer 20 by evaporating the liquefied gas, separating the heavy carbon holding the liquid, and improving the quality of the liquefied gas supplied to the customer 20. .

  At this time, the gas-liquid separator 51 may be referred to as a mist separator, a heavy carbon separator, or the like, and the liquid heavy carbon returns to the liquefied gas storage tank 10 or is transmitted to a separately provided tank. For this reason, the gas-liquid separator 51 may be provided with a heavy carbon return line (not shown) connected to the liquefied gas storage tank 10.

  The heater 52 heats the liquefied gas from which the heavy carbon is separated. The forced vaporizer 50 heats the liquefied gas, but since the vaporized liquefied gas has a temperature (for example, −100 degrees) for causing the heavy carbon to remain in a liquid state, the temperature required by the customer 20 is not reached. There is.

  Accordingly, similarly to the forced vaporizer 50, the heater 52 can heat the liquefied gas using various heat sources, and at this time, the heat source is shared with the forced vaporizer 50 and / or the vaporizer 42. Can do.

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

  Although the liquefied gas is stored in the liquefied gas storage tank 10, foreign substances may be mixed into the liquefied gas inside the liquefied gas storage tank 10 due to various fluids returning from the outside. Therefore, the strainer can remove the foreign matters mixed in the liquefied gas, and the pure liquefied gas can be transmitted to the forced vaporizer 50.

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

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

  The H / D compressor 36 may be used for the purpose of discharging the evaporated gas generated in the liquefied gas storage tank 10 when bunkering to the outside or compressing it for incineration. Not limited.

  The reliquefaction device 37 can reliquefy excess evaporating gas with a reliquefied refrigerant and return it to the liquefied gas storage tank 10. The reliquefaction device 37 may include a reliquefaction heat exchanger (not shown) and a reliquefaction refrigerant supply device (not shown).

  The reliquefaction device 37 supplies cold heat for reliquefying the evaporated gas through the reliquefaction refrigerant supply device, and the refrigerant supplied from the reliquefaction refrigerant supply device is supplied to the reliquefaction heat exchanger by another pump (not shown). Then, cold heat can be supplied to the evaporating gas to reliquefy.

  The return pump 38 can supply the liquid state to the liquefied gas storage tank 10 via the tenth line L10 from the gas-liquid separator 35 that separates the evaporated gas re-liquefied by the re-liquefaction device 37 into a liquid state and a gas state. .

  At this time, in the present invention, when the liquid is not supplied from the gas-liquid separator 35 to the liquefied gas storage tank 10 (the supply of liquid is interrupted by the pressure difference between the internal pressures of the gas-liquid separator 35 and the liquefied gas storage tank 10). ), The liquid state of the gas-liquid separator 35 can be supplied to the liquefied gas storage tank 10 via the eleventh line L11 as a bypass line, a bypass valve (not shown), and the return pump 38.

  Specifically, when the liquid evaporative gas stored in the gas-liquid separator 35 is stored at a pressure larger than the internal pressure of the liquefied gas storage tank 10, it is supplied to the liquefied gas storage tank 10 via the tenth line L10. When the liquid evaporative gas stored in the first gas-liquid separator 35 is stored at a pressure lower than the internal pressure of the liquefied gas storage tank 10, the liquefied gas is driven by driving the reliquefaction supply pump 38. The storage tank 10 can be supplied.

  Below, the Example of the gas processing system which can be derived | led-out through each structure mentioned above is described.

  The gas processing system 1 according to the embodiment of the present invention may further include a configuration in which the liquefied gas or the evaporated gas is processed and supplied to the customer 20 by the individual configuration described above.

  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 will be described in detail.

  First, the processing mechanism of the liquefied gas stored in the liquefied gas storage tank 10 will be described. The gas processing system 1 according to the embodiment of the present invention supplies the liquefied gas stored in the liquefied gas storage tank 10 along the first line L1. The primary pressure is applied using the boosting pump 40 while supplying to the customer 20, and then the impurities of the liquefied gas are removed by a strainer (not shown), and then a) forced vaporization along the sixth line L6. B) can be supplied to the high pressure pump 41 along the first line L1.

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

  b) The liquefied gas supplied to the high pressure pump 41 along the first line L1 may be pressurized to a high pressure by the high pressure pump 41 and vaporized by the vaporizer 42, and then supplied to the high pressure customer 21.

  The processing mechanism of the evaporative gas generated in the liquefied gas storage tank 10 will be described. The gas processing system 1 according to the embodiment of the present invention converts the evaporative gas generated in the liquefied gas storage tank 10 into c) the second line L2 or d). Multi-stage pressurization using the evaporative gas compressor 30 along the third line L3 can be performed and supplied to the customer 20.

  c) The evaporative gas supplied through the second line L2 may be multi-stage compressed to a high pressure by the evaporative gas compressor 30 and supplied to the high-pressure customer 21 and is vaporized at a high pressure through the process b) described above. The liquefied gas may be merged and supplied to the high-pressure customer 21 together.

  d) The evaporative gas supplied via the third line L3 is an evaporative gas supplied by branching the evaporative gas supplied via the second line L2 in two or three stages of the evaporative gas compressor 30. Thus, it may be supplied to the low-pressure customer 22 or may be supplied to the low-pressure customer 22 by joining with the liquefied gas forcedly vaporized through the process a) described above.

  At this time, the forcibly vaporized liquefied gas supplied by the forcible vaporizer 50 may be supplied when the fuel consumption amount of the low-pressure demand destination 22 increases, but is not limited to this example. (The liquefied gas stored in the liquefied gas storage tank 10 has a high composition ratio of heavy carbon, so that the heavy carbon is liquefied by using the forced vaporizer 50 and the gas-liquid separator 51 to lower it. It is also possible to increase the efficiency of the low-pressure customer 22 by supplying only the gas to the low-pressure customer 22.)

  As described above, the evaporative gas generated in the liquefied gas storage tank 10 may be supplied to the gas combustion device 23 and the vent mast 24. In this case, the evaporative gas is provided on the line via another line (not shown). The gas combustion device 23 or the vent mast 24 may be supplied through a valve (not shown).

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

  The evaporative gas generated in the liquefied gas storage tank 10 according to the embodiment of the present invention is supplied to the consumption destination 20 of the evaporative gas when the internal pressure of the liquefied gas storage tank 10 is equal to or higher than a preset pressure. Is stored in the liquefied gas storage tank 10 when the internal pressure is less than the preset pressure. Here, the preset pressure may be 1.06 bar to 1.12 bar, and the consumption destination 20 of the evaporative gas includes the gas combustion device 23 and the vent mast 24, and the internal pressure of the liquefied gas storage tank 10 is preset. When the pressure is less than the pressure, the driving of the engine 20 that generates the propulsive force of the ship (not shown) may be 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 less than a preset pressure, the operation of the evaporative gas compressor 30 is stopped, and the evaporative gas generated in the liquefied gas storage tank 10 Can be stored in the liquefied gas storage tank 10 as it is.

  In an embodiment of the present invention, when the internal pressure of the liquefied gas storage tank 10 is equal to or higher than a preset pressure, more specifically, when the internal pressure of the liquefied gas storage tank 10 is 1.17 bar to 1.20 bar, The evaporative gas generated in the liquefied gas storage tank 10 is pressurized by the evaporative gas compressor 30 and supplied to the gas combustion device 23 for burning the evaporative gas. The internal pressure of the liquefied gas storage tank 10 is 1.20 bar to 1.25 bar. In some cases, evaporative gas generated in the liquefied gas storage tank 10 is supplied to a vent mast (Vent Mast) and 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 is stored. Evaporated gas generated in the tank 10 is supplied to a safety valve (not shown; Safety Valve), and the inside of the liquefied gas storage tank 10 is supplied via the safety valve. Can be discharged to the outside.

  As described above, in the embodiment of the present invention, the evaporative gas generated in the liquefied gas storage tank 10 is accumulated up to a preset pressure, so that the evaporative gas is discharged to the outside and burned to be combusted. Therefore, it is possible to reduce power consumption and not to release the evaporated gas to the outside.

  The gas processing system 1 according to the embodiment of the present invention may include a technology that enables the H / D compressor 36 to be used in common during 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 that pressurizes evaporative gas generated in the liquefied gas storage tank 10, and a heater that heats the evaporative gas compressed by the H / D compressor 36 ( (Not shown) and an on-shore storage (Shore) where liquefied gas to be supplied to the liquefied gas storage tank 10 during bunkering is stored, or temporary storage for temporarily storing evaporative gas generated in the liquefied gas storage tank 10 during bunkering (Not shown) as a main configuration.

  When the liquefied gas is first loaded into the liquefied gas storage tank 10 from the outside (including when the liquefied gas is loaded after the maintenance work of the liquefied gas storage tank 10 is completed), that is, during bunkering, Considering the fact that it is a cryogenic pyrophoric material, a special operation different from a general storage tank, that is, a replacement operation must be preceded.

  Generally, the replacement method for the liquefied gas storage tank 10 is to supply dry gas into the liquefied gas storage tank 10 to remove moisture and store the inert gas in the liquefied gas to eliminate the possibility of a fire or explosion. Supplying the inside of the tank 10 removes oxygen. Thereafter, a cool-down process is performed in which the hydrocarbon gas is supplied into the liquefied gas storage tank 10 to remove the inert gas, and the liquefied gas is used to cool the liquefied gas storage tank 10. The When the cool-down process is completed, the replacement method is completed, and thereafter, a liquefied gas such as LNG is supplied into the liquefied gas storage tank 10 to perform a loading operation.

  Conversely, when the liquefied gas stored in the liquefied gas storage tank 10 is unloaded to the shore demand (Shore) (including the case where all of the liquefied gas is removed before the maintenance work of the liquefied gas storage tank 10). ) Is slightly different from the above process.

  First, all the liquefied gas stored in the liquefied gas storage tank 10 is discharged to a customer (Shore). At this time, although there is residual liquefied gas, a warm-up stage is performed in order to remove all residual liquefied gas. In the warm-up stage, after evaporating gas generated in the liquefied gas storage tank 10 is compressed by a compressor, it is heated by another heater and returned to the liquefied gas storage tank 10 again, whereby the internal temperature of the liquefied gas storage tank 10 is restored. To evaporate any remaining liquefied gas. After the warm-up stage, in order to remove all the evaporated gas remaining in the liquefied gas storage tank 10, an inert gas is supplied, a drying gas is supplied to dry the inside, and then oxygen is supplied to the inside. Supply air. Through the above process, the unloading process of the liquefied gas storage tank 10 is completed, and then an operator for performing maintenance work and the like can enter.

  Here, during the liquefied gas loading process (during bunkering), even if the liquefied gas storage tank 10 is cooled down, a large amount of evaporative gas is generated when the liquefied gas is loaded. At this time, the liquefied gas storage tank 10 Since the internal pressure may increase, a compressor is used to discharge the generated evaporated gas to the outside.

  In the warm-up stage of the liquefied gas unloading process, a compressor is used in the process of compressing the evaporative gas in order to raise the internal temperature of the liquefied gas storage tank 10.

  As described above, the H / D compressor 36 can realize both the compression process used in the liquefied gas loading process and the compression process used in the liquefied gas unloading process.

  That is, the H / D compressor 36 pressurizes the evaporated gas generated at the time of bunkering and supplies it to the shore demand (Shore) or warms the liquefied gas at the unloading time (before the maintenance of the liquefied gas storage tank 10). The evaporative gas remaining in the liquefied gas storage tank 10 can be pressurized and returned to the liquefied gas storage tank 10 again in the up stage, and the evaporative gas can be circulated to the liquefied gas storage tank 10.

  Specifically, the H / D compressor 36 receives and compresses the evaporative gas generated in the liquefied gas storage tank 10 via the seventh line L7 during bunkering, and supplies the compressed gas to the shore demand (Shore). When the liquefied gas is unloaded (before the liquefied gas storage tank 10 is maintained), the evaporated gas remaining in the liquefied gas storage tank 10 is compressed and heated by the heater 361, and then the eighth line L8 The liquefied gas storage tank 10 is returned to the liquefied gas storage tank 10 through the twelfth line L12, and the evaporated gas can be circulated in the order of the liquefied gas storage tank 10, the H / D compressor 36, the heater 361, and the liquefied gas storage tank 10. Thereby, all the liquefied gas stored in the liquefied gas storage tank 10 can be vaporized, and all 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 is used for compressing the evaporative gas generated during bunkering and discharging it to a shore demand (Shore), and at the time of unloading the liquefied gas (maintenance of the liquefied gas storage tank 10). Used to increase the temperature of the remaining evaporating gas and pressurize the liquefied gas storage tank 10 to circulate in order to vaporize all the remaining liquefied gas stored in the liquefied gas storage tank 10. May be.

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

  The gas processing system 1 according to the embodiment of the present invention further includes a pressure reducing valve 341 together with the reliquefaction device 37 to improve the reliquefaction rate, and bypass the return pump 38 according to the internal pressure of the gas-liquid separator 35. And a technology for sharing a line through which evaporative gas is supplied to the GCU 23 and the reliquefaction device 37 may be included.

  The gas processing system 1 according to the embodiment of the present invention includes an evaporative gas compressor 30 that pressurizes evaporative gas generated in the liquefied gas storage tank 10 in multiple stages, and a re-liquefied evaporative gas compressed by the evaporative gas compressor 30 with a refrigerant. A liquefying device 37; a first pressure reducing valve 341 for depressurizing or expanding the evaporated gas compressed by the evaporative gas compressor 30; and a second pressure reducing valve for depressurizing or expanding the evaporated gas at least partially liquefied through the reliquefaction device. 342 and a gas-liquid separator 35 that maintains the pressure obtained by secondary depressurization of the evaporated gas re-liquefied by the second pressure reducing valve 342 and separates the gas into liquid and liquid state as main components.

  Here, the reliquefaction device 37 can liquefy the evaporated gas that has been branched at the intermediate stage of the evaporated gas compressor 30 and compressed to a low pressure (13 bar to 15 bar) with a refrigerant, and more specifically, the evaporated gas. The evaporative gas branched at the intermediate stage of the compressor 30 and compressed to a low pressure (13 bar to 15 bar) is primarily decompressed to 7 bar to 8 bar by the first pressure reducing valve 341, and then cooled through the reliquefaction device 37 to be cooled. The evaporated gas may be secondarily depressurized to 5 to 6 bar by the second pressure reducing valve 342.

  Thus, in the Example of this invention, the pressure reducing valve 342 is further provided in the back | latter stage of the reliquefaction apparatus 37, and reliquefaction efficiency can be improved further conventionally.

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

  Specifically, the liquid liquefied gas stored in the gas-liquid separator 35 is liquefied via the return line (tenth line) L10 when the internal pressure of the gas-liquid separator 35 is equal to or higher than a preset pressure value. When supplied to the gas storage tank 10 and the internal pressure of the gas-liquid separator 35 is lower than the preset pressure value, the return pump 38 is driven to store the liquefied gas via the bypass line (11th line) L11. It can be supplied to the tank 10.

  That is, since the gas-liquid separator 35 stores the evaporated gas that has been secondarily reduced to 5 to 6 bar by the second pressure reducing valve 342, the liquid-reduced evaporated gas is larger than the internal pressure of the liquefied gas storage tank 10. Since it can be naturally supplied by a pressure gradient that is a physical law, when the internal pressure of the gas-liquid separator 35 is equal to or higher than a preset pressure value, it is supplied to the liquefied gas storage tank 10 via the return line L10. By doing so, there is an effect that the driving power consumption of the return pump 38 can be prevented and the return to the stable liquefied gas storage tank 10 can be realized.

  Further, the branch line is branched at the intermediate stage of the evaporative gas compressor 30 when the supply amount of the evaporative gas branched at the intermediate stage of the evaporative gas compressor 30 and compressed to a low pressure is larger than the preset supply amount. At least a part of the evaporative gas compressed to a low pressure is supplied to the gas combustion device 23, and the supply amount of the evaporative gas branched at the intermediate stage of the evaporative gas compressor 30 and compressed to the low pressure is smaller than the preset supply amount. In this case, it is possible to supply all of the evaporating gas branched at the intermediate stage of the evaporating gas compressor 30 and compressed to a low pressure to the reliquefaction device 37.

  That is, by providing both the first pressure reducing valve 341 and the second pressure reducing valve 342 on the fourth line L4, it is not necessary to provide a separate side stream line of the evaporative gas compressor 30 in addition to the fourth line L4. The branching line of the evaporative gas compressor 30 can be minimized, thereby improving the driving reliability of the system. (When the side stream line of the evaporative gas compressor 30 increases, the driving efficiency decreases.)

  Here, the preset pressure value may be 5 to 6 bar, the reliquefaction device 37 may use nitrogen as a refrigerant, and the second pressure reducing valve 342 may be a Joule-Thompson 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 customer 21 and the technology for supplying the low-pressure customer 22 without another decompression. Technology that can be used may be included.

  The gas processing system 1 according to the embodiment of the present invention includes a boosting pump 40 that primarily pressurizes the liquefied gas stored in the liquefied gas storage tank 10, and a supply of the liquefied gas primarily pressurized from the boosting pump 40. The high pressure pump 41 that receives and pressurizes the second pressure, the vaporizer 42 that receives the supply of the second pressurized gas from the high pressure pump 41 and vaporizes, and the high pressure liquefied gas or evaporative gas compressed from the vaporizer 42. High-pressure demand 21 that receives and consumes the supply of pressurized evaporative gas from the machine 30, and low-pressure that consumes the supply of evaporative gas that has been branched at the intermediate stage of the evaporative gas compressor 30 and pressurized to a low pressure A forced vaporizer 50 for receiving and supplying the liquefied gas stored in the liquefied gas storage tank 10 to forcibly vaporize, and between the forced vaporizer 50 and the low-pressure customer 22 for forced vaporization Including a gas-liquid separator 51 for separating the gaseous and liquid receives a supply of forced vaporized liquefied gas 50, as main components.

  The boosting pump 40 primarily pressurizes the liquefied gas stored in the liquefied gas storage tank 10 and supplies the liquefied gas to the high pressure pump 41 or the forced vaporizer 50, and supplies the high pressure pump 41 and the forced vaporizer 50 through the boosting pump 40. You can share the use of pumps.

  Here, the forced vaporizer 50 receives and vaporizes the liquefied gas stored in the liquefied gas storage tank 10 while being primarily pressurized from the boosting pump 40, and then supplies the vaporized gas to the low-pressure customer 22. Thus, the fuel can be supplied to the low-pressure customer 22 without further decompression. Thereby, in a present Example, there exists an effect which can omit installing a pressure-reduction valve in the inflow end of the low voltage | pressure customer 22.

  Further, the forced vaporizer 50 receives the vaporized liquefied gas stored in the liquefied gas storage tank 10 in a state where it is primarily pressurized from the boosting pump 40 and vaporizes the liquefied gas before the evaporative gas compressor 30. Can be supplied. In this embodiment, since the evaporative gas compressor 30 adjusts the required pressure of the demand destination 20, there is an effect that the delivery pressure of the boosting pump 40 can be lowered. Of course, also in this case, the liquefied gas supplied to the forced vaporizer 50 may be supplied through the boosting pump 40 that supplies the liquefied gas to the high-pressure pump 41.

  Thus, by sharing the use of the pump supplied to the high-pressure pump 41 and the forced vaporizer 50 by the boosting pump 40, there is an effect of reducing the construction cost of the pump 40, and the forced vaporization is performed through the forced vaporizer 50. By supplying the evaporated gas to the front stage of the evaporated gas compressor 30, the liquefied gas delivery pressure from 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 in the subsequent stage of the return line L10 of the gas-liquid separator 35 provided in the subsequent stage of the reliquefaction device 37, the cool-down circulation line L13 of the high-pressure pump 41, and the forced vaporizer 50. A technique of sharing at least one return line (not shown) of the gas-liquid separator 51 may be included.

  The gas processing system 1 according to the embodiment of the present invention includes a reliquefaction device 37 for reliquefying the evaporative gas compressed by the evaporative gas compressor 30, and the evaporative gas reliquefied by the reliquefaction device 37 in a gaseous state and a liquid state. The gas-liquid separator 35 to be separated, the high-pressure pump 41 that pressurizes the liquefied gas stored in the liquefied gas storage tank 10, and the forced vaporizer 50 that forcibly vaporizes the liquefied gas are gasified and liquefied. When the high pressure pump 41 is cooled down, the cool down circulation line (13th line) L13 connected from the high pressure pump 41 to the liquefied gas storage tank 10 and the liquid state of the gas liquid separator 35 are separated. Of the gas-liquid separator 35 for returning the gas to the liquefied gas storage tank 10 and the gas-liquid separator for returning the liquid state of the gas-liquid separator 51 to the liquefied gas storage tank 10. It includes a first return line (not shown), as the main components.

  In the embodiment of the present invention, when the high pressure pump 41 is cooled down, the line L13 for returning the high pressure pump 41 to the liquefied gas storage tank 10 and the line L10 for returning the liquid state of the gas-liquid separator 35 to the liquefied gas storage tank 10; At least one line for returning the liquid state of the gas-liquid separator 51 to the liquefied gas storage tank 10 may be shared.

  Thus, the structure of the return line is simplified by sharing at least one of the cool-down circulation line L13 of the high-pressure pump 41, the return line L11 of the gas-liquid separator 35, and the return line of the gas-liquid separator 51. As a result, the driving reliability of the system is improved, and the return is stably realized. Since the return line is shared and the cool-down can be performed in advance, the liquid evaporative gas is stored in the liquefied gas. There is an effect of not re-vaporizing while returning to the tank 10. That is, there is an effect that the substantial reliquefaction efficiency is increased.

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

  When the high pressure customer 21 is driven through the liquefied gas and the evaporated gas is reliquefied by the reliquefaction device 37 at the same time, the discharge pressure of the gas-liquid separator 35, that is, the pressure of the return line L10 is The cool-down circulation line L13 of the high-pressure pump 41 corresponds to about 9 bar. In the case of the return line L10, there may occur a problem that a reverse pressure is applied and the gas-liquid separator 35 flows backward.

  However, in the embodiment of the present invention, the high pressure pump 21 is driven by the liquefied gas and the evaporation gas is not reliquefied by the reliquefaction device 37 at the same time. Only the return line of the down circulation line L13 and the gas-liquid separator 35 can be shared to prevent reverse pressure on the shared line, and the return line can be effectively shared. (When the reliquefaction device 37 is driven, it is a case where evaporative gas remains, but in this case, since the evaporative gas is supplied to the high-pressure demand destination 21 through the evaporative gas compressor 30, (There is no need to send the liquefied gas to the high-pressure customer 21 through the high-pressure pump 41, and the high-pressure pump 41 is not driven.)

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

  The forced vaporizer 50 operates only when the low-pressure demand destination 22 is driven, and the high-pressure pump 41 operates only when the high-pressure demand destination 21 is driven. Therefore, all the high-pressure and low-pressure demand destinations 21 and 22 operate. Only in this case, the cool-down circulation line L13 of the high-pressure pump 41 and the return line of the gas-liquid separator 51 can be shared.

  As a result, the return line of the gas-liquid separator 51 is cooled in advance by the cool-down of the high-pressure pump 41, and the liquid that returns from the gas-liquid separator 51 to the liquefied gas storage tank 10 is not re-vaporized. The internal pressure of the tank 10 can be managed efficiently. Of course, at this time, the return line of the gas-liquid separator 51 and the cool-down circulation line L13 of the high-pressure pump 41 differ from each other at the time of flow, so that the problem of back pressure does not occur. (The cool-down of the high-pressure pump 41 is driven only in the initial stage of supply to the high-pressure customer 21, and the return line of the gas-liquid separator 51 is continuously driven while being supplied to the low-pressure customer 22.)

  The gas processing system 1 according to the embodiment of the present invention may include a technique for facilitating the cool-down of the return line of the gas-liquid separator 51 by connecting the preceding stage of the forced vaporizer 50 to the return line of the gas-liquid separator 51. Good.

  A gas processing system 1 according to an embodiment of the present invention includes a gas-liquid separator 51 that separates a liquefied gas forcedly vaporized by a forced vaporizer 50 that forcibly vaporizes the liquefied gas into gas and liquid, and a gas-liquid separator 51. Main components are a return line of the gas-liquid separator 51 for returning the liquid state to the liquefied gas storage tank 10, and a bypass line (not shown) connecting the preceding stage of the forced vaporizer 50 and the return line of the gas-liquid separator 51. Include as.

  In the embodiment of the present invention, a bypass line connecting the upstream stage of the forced vaporizer 50 and the return line of the gas-liquid separator 51 is provided, and both the bypass line of the forced vaporizer 50 and the return line of the gas-liquid separator 51 are shared. can do.

  As a result, the bypass line of the forced vaporizer 50 is connected to the return line of the gas-liquid separator 51 that is not the previous stage of the gas-liquid separator 51, and the bypass function of the forced vaporizer 50 and the return line cool of the gas-liquid separator 51 are connected. The down function can be shared, and the cool-down of the gas-liquid separator 51 can be simplified and optimized.

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

  Hereinafter, description will be made with reference to FIGS. 2A to 2C. However, 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 processing system of the present invention.

  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 are vaporizers (vaporization heat exchange) for vaporizing the liquefied gas stored in the liquefied gas storage tank 10 with a vaporized heat medium. 424), a first heat exchanger (first supply device for the vaporized heat medium) 4231 for exchanging heat between the vaporized heat medium and the engine coolant, and a second heat exchanger (heat for vaporization) for supplying a heat source to the vaporized heat medium. Medium second supply device) 4232 and a circulation pump 422 for circulating the vaporized heat medium so as to supply the vaporizer 424 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 supply device 4231 for the vaporization heat medium and the second supply device 4232 for the vaporization heat medium. Can supply the heat source to the vaporization heat medium in the order of the first supply device 4231 of the vaporization heat medium and the second supply device 4232 of the vaporization heat medium, and more specifically, the circulation pump 422, the first of the vaporization heat medium. The first supply device 4231 and the second supply device 4232 for vaporization heat medium may be connected in series in this order, or the first supply device 4231 for vaporization heat medium, the circulation pump 422, and the second supply device 4232 for vaporization heat medium may be connected in series. Good.

  Here, the first supply device 4231 for vaporization heat medium and the second supply device 4232 for vaporization heat medium are the plate type, and the second supply device 4232 for vaporization heat medium is the Shell & Tube method. The types of heat exchangers may be different from each other. It goes without saying that the two heat exchangers may be used in the same type as the Plate system or the Shell & Tube system. Moreover, the 2nd supply apparatus 4232 of a vaporization heat medium may use steam or seawater as a heat source supplied to a vaporization heat medium.

  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 supply of the vaporized heat medium is connected to the front stage and the rear stage of the first supply unit 4231 of the vaporized heat medium. The first bypass line (first branch line of the vaporized heat medium) GBL1 for bypassing the vaporized heat medium having passed through the apparatus 4231 from the rear stage to the front stage of the first supply apparatus 4231 of the vaporized heat medium, the second supply apparatus 4232 of the vaporized heat medium A second bypass line (second branch of the vaporized heat medium) that bypasses the vaporized heat medium that has been connected to the front stage and the rear stage and passed through the second supply apparatus 4232 of the vaporized heat medium from the rear stage to the front stage of the second supply apparatus 4232 of the vaporized heat medium. Line) GBL2, and controller 902 for controlling first bypass line GBL1 or second bypass line GBL2, and vaporized heat medium storage tank 421 for storing the vaporized heat medium may further be included.

  When the vaporization heat medium supplied to the vaporizer 424 is equal to or lower than a preset temperature value, the controller 902 drives the vaporization heat medium first branch line GBL1 or the vaporization heat medium second branch line GBL2, The vaporized heat medium can be reheated. Here, the preset temperature value is 85 degrees to 95 degrees, and the second supply device 4232 for the vaporization heat medium is supplied with a heat source according to the heat source supply capability of the first supply device 4231 for the vaporization heat medium. Good.

  In the first embodiment 42a of the vaporizer of the gas processing system according to an embodiment of the present invention, the process of heating / cooling the vaporized heat medium will be described. The vaporized heat medium stored in the vaporized heat medium storage tank 421 is described below. Can be circulated through the vaporization heat medium circulation pump 422, heated by the engine cooling water (jacket cooling water) by the vaporization heat medium first supply device 4231 and heated up to 70 degrees, and then the vaporization heat medium The second supply device 4232 and heated by steam or sea water to about 85 to 95 degrees (preferably 90 degrees), and then supplied to the vaporization heat exchanger 424 to -130 degree liquefied gas flowing through line L1 can be heated to 35 to 55 degrees, and the vaporized refrigerant can be cooled to 90 to 50 degrees. That.

  Here, the engine cooling water is supplied by the first supply device 4231 for the vaporized heat medium, and the amount of engine cooling water at the time of heating changes according to the driving of the engine. Therefore, the second supply device 4232 for the vaporized heat medium can be heated in a variable manner depending on the first supply device 4231 for the vaporized heat medium. This may be realized by driving the control unit 902 described above. The control unit 902 transmits the temperature information of the liquefied gas or the vaporized heat medium from the first temperature measuring device 921 and the second temperature measuring device 922 by wire or wirelessly. Based on this, the vaporizing heat medium can be heated by driving the first bypass line GBL1 or the second bypass line GBL2 in accordance with the situation described above.

  In the second embodiment 42b of the vaporizer of the gas processing system 1 according to the embodiment of the present invention, a process of heating / cooling the vaporized heat medium will be described. First supply device 4231 of the vaporized heat medium and the vaporized heat medium Only the order of the circulation pump 422 is changed, and the rest is the same as the description of the first embodiment 42a of the vaporizer described above, and therefore, this is replaced.

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

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

  A third embodiment 42c of the vaporizer of the gas processing system 1 according to an embodiment of the present invention includes a vaporization heat exchanger 424, a first supply device 4231 for vaporization heat medium, a second supply device 4232 for vaporization heat medium, A circulation pump 422 and a heater (additional heater for vaporization heat medium) 4233 which is provided at the subsequent stage of the vaporization heat medium first supply device 4231 and further heats the vaporization heat medium heated by the first vaporization heat medium supply device 4231. And the vaporization heat medium heated by the vaporization heat medium first supply device 4231 is supplied to the preceding stage of the vaporization heat medium second supply device 4232. And a bypass line (third branch line of the vaporized heat medium) GBL4.

  The first supply device 4231 for vaporization heat medium and the second supply device 4232 for vaporization heat medium are connected in parallel with the first supply device 4231 for vaporization heat medium and the second supply device 4232 for vaporization heat medium. The first supply device 4231 first heats the vaporization heat medium, and the second supply device 4232 of the vaporization heat medium can heat the vaporization heat medium later. The first supply device 4231 and the vaporization heat medium of the vaporization heat medium can be heated. The second supply device 4232 may be disposed at the subsequent stage of the circulation pump 422.

  Specifically, the vaporization heat medium heated by the first supply device 4231 of the vaporization heat medium is vaporized by the heater 4233 when the temperature of the subsequent stage of the first supply device 4231 of the vaporization heat medium is equal to or lower than a preset temperature. The heat medium can be heated or supplied to the front stage of the second supply device 4232 for the vaporized heat medium via the bypass line GBL4.

  Here, the first supply device 4231 for the vaporized heat medium is a Plate method, and the second supply device 4232 for the vaporized heat medium is a Shell & Tube method, and the types of the two heat exchangers may be different. It goes without saying that the same type as the plate system or the Shell & Tube system may be used. The second supply device 4232 for the vaporized heat medium may use steam or seawater as a heat source supplied to the vaporized heat medium.

  In the third embodiment 42c of the vaporizer of the gas processing system 1 according to the embodiment of the present invention, a process of heating / cooling the vaporized heat medium will be described. The vaporized heat medium stored in the vaporized heat medium storage tank 421 is described below. Can be circulated through the vaporization heat medium circulation pump 422 and heated by engine cooling water (jacket cooling water) by the vaporization heat medium first supply device 4231 to be heated up to 90 degrees.

  However, since the amount of engine cooling water changes according to the driving of the engine, it is difficult to supply a constant heat source to the vaporization heat exchanger 424 because the temperature changes drastically. In order to prevent this, the present invention may further include an additional heater 4233 for the vaporization heat medium. In the present invention, when the engine is driven at a low speed and the heat source supply amount of the engine cooling water decreases, it can be heated up to 90 degrees by reheating with the additional heater 4233 of the vaporized heat medium. Thereafter, the -130 degree liquefied gas that is supplied to the vaporization heat exchanger 424 and flows through the first line L1 can be heated to 35 to 55 degrees, and the vaporized refrigerant is cooled to 90 degrees to 50 degrees. be able to.

  Here, the second supply device 4232 for the vaporized heat medium can be varied and heated according to the first supply device 4231 for the vaporized heat medium. This can be realized by driving the control unit 902 described above. The control unit 902 transmits the temperature information of the liquefied gas or the vaporized heat medium from the first temperature measuring device 921 and the second temperature measuring device 922 by wire or wirelessly. Based on this, the first bypass line GBL1 or the second bypass line GBL2 can be driven to heat the vaporized heat medium according to the above-described situation.

  Also, the second supply device 4232 of the vaporization heat medium stops the drive of the engine for a long time, the supply of engine cooling water becomes very small, and the amount of heat generated by the additional heater 4233 of the vaporization heat medium is not sufficient. Since the medium is supplied to the vaporization heat medium circulation line GL without being supplied to the third branch line GBL3 of the vaporization heat medium, the vaporization heat medium can be heated to 90 degrees.

  The amount of engine cooling water in the third embodiment 42c of the carburetor according to an embodiment of the present invention varies depending on the driving of the engine. It is bypassed to the vaporization heat medium second supply device 4232 via the branch line GBL4 and can be heated to 90 degrees by the vaporization heat medium second supply device 4232.

  By connecting the above-described vaporized heat medium supply devices in parallel or in series, the flow rate of the steam is reduced by the engine cooling water through the heating technique of the vaporized heat medium, and the operation of the boiler is reduced, thereby reducing fuel consumption. In addition, by connecting in series or in parallel, the driving reliability of the carburetor 42 is improved.

  The gas processing system 1 according to the embodiment of the present invention may include a technology that realizes processing of liquefied gas and evaporative gas in parallel 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 apparatus that pressurizes / heats the liquefied gas stored in the liquefied gas storage tank 10 and supplies the liquefied gas to a customer. 40, 41, 42, a re-liquefaction device 37 for re-liquefying the evaporative gas compressed by the evaporative gas compressor 30, and a reduced pressure of the evaporative gas liquefied by the re-liquefaction device 37 provided at the subsequent stage Or the 2nd pressure-reduction valve 342 to expand, the gas combustion apparatus 23 which consumes evaporative gas, and the forced vaporizer 50 which forcibly vaporizes the liquefied gas stored in the liquefied gas storage tank 10 are included as main structures.

  Here, the liquefied gas processing devices 40, 41, and 42 supply a boosting pump 40 for primarily pressurizing the liquefied gas stored in the liquefied gas storage tank 10, and supply of the liquefied gas pressurized from the boosting pump 40. The evaporative gas compressor 30 is provided in parallel, and includes a high-pressure pump 41 that receives and secondarily pressurizes, and a vaporizer 42 that receives the supply of the liquefied gas pressurized to a high pressure from the high-pressure pump 41 and vaporizes it. The first evaporative gas compressor (not shown) and the second evaporative gas compressor (not shown) may be provided.

  Below, the 1st parallel drive of the gas processing system 1 according to the internal pressure of the liquefied gas storage tank 10 is demonstrated.

  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 second preset pressure is the first preset pressure. Greater than 1,12 bar, the third preset pressure is less than the first preset pressure and greater than 1.06 bar, and the fourth preset pressure is less than the third preset pressure and less than 1 It may be greater than 0.03 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 preset pressure, the second evaporative gas compressor is further driven, and when the internal pressure of the liquefied gas storage tank 10 is less than the first preset pressure, The gas processing devices 40, 41 and 42 are further driven.

  The evaporative gas generated in the liquefied gas storage tank 10 may be supplied to the reliquefaction device 37 or the gas combustion device 23 when the internal pressure of the liquefied gas storage tank 10 is equal to or higher than the second preset pressure. In addition to the case where the internal pressure of the tank 10 is equal to or higher than the second preset pressure, the liquefied gas processing devices 40, 41, and 42 are further driven when the required fuel amount of the customer 20 is equal to or higher than the preset required amount. Can do.

  Further, when the internal pressure of the liquefied gas storage tank 10 is less than the third preset pressure, the driving of the first evaporative gas compressor may be stopped, and the internal pressure of the liquefied gas storage tank 10 is set to the fourth preset pressure. If it is less, the liquefied gas stored in the liquefied gas storage tank 10 is forcibly vaporized by the forced vaporizer 50, and the liquefied gas that has been forcibly vaporized is returned to the liquefied gas storage tank 10 again. Can be raised.

  At this time, in the embodiment of the present invention, a control unit (not shown) and a pressure measuring device (not shown) for measuring the internal pressure of the liquefied gas storage tank 10 and a fuel requirement measurement for measuring the fuel requirement of the customer 20 are measured. The controller may further include a device (not shown), and the control unit receives information from the pressure measurement device and the fuel requirement measurement device in a wired or wireless manner, and receives the first internal pressure of the liquefied gas storage tank 10 described above. The liquefied gas processing devices 40, 41, and 42 and the evaporative gas compressor 30 can be controlled with respect to fluctuations caused by the fourth preset pressure.

  As described above, in the embodiment of the present invention, the evaporative gas compressor 30 and the liquefied gas processing devices 40, 41, and 42 are driven in parallel so that the customer 20 can be driven flexibly without oil supply. This has the effect of reducing system construction costs.

  When the internal pressure of the liquefied gas storage tank 10 is low, the gas processing system 1 according to the embodiment of the present invention includes a technique for realizing the processing of the liquefied gas, the evaporated gas, and the oil in parallel by the flow of the internal pressure. Good.

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

  Below, the 2nd parallel drive of the gas processing system 1 according to the internal pressure of the liquefied gas storage tank 10 is demonstrated.

  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 fuel requirement of the customer 20, the reliquefaction device 37 is further operated. When the amount of evaporative gas generated in the liquefied gas storage tank 10 is smaller than the required fuel amount of the customer 20, the liquefied gas processing devices 40, 41, 42 and the oil processing device may be further operated. Preferably, the liquefied gas processing devices 40, 41, 42 can be operated first, and the oil processing device can be operated next.

  Here, the first preset pressure is the internal pressure of the liquefied gas storage tank 10 when the BOR (Boiled Off Rate) in the liquefied gas storage tank 10 is 75 to 85%, or 1.06 bar to 1 It may be .12 bar.

  At this time, in the embodiment of the present invention, the control unit receives information from the pressure measurement device and the fuel requirement measurement device by wire or wirelessly, and the first preset value of the internal pressure of the liquefied gas storage tank 10 described above. The liquefied gas processing devices 40, 41 and 42, the evaporative gas compressor 30 and the oil processing device can be controlled with respect to fluctuations due to the pressure of the gas.

  As described above, in the embodiment of the present invention, the evaporative gas compressor 30, the liquefied gas processing devices 40, 41 and 42, and the oil processing device can be driven in parallel to satisfy the fuel supply constancy of the system. The driving reliability is improved.

  When the internal pressure of the liquefied gas storage tank 10 is high, the gas processing system 1 according to the embodiment of the present invention includes a technique for realizing the processing of the liquefied gas, the evaporating gas, and the oil in parallel by the flow of the internal pressure. Good.

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

  Below, the control drive of the gas processing system 1 according to the internal pressure of the liquefied gas storage tank 10 is demonstrated.

  When the internal pressure of the liquefied gas storage tank 10 is equal to or higher than the preset pressure, the first evaporative gas compressor is operated and supplied to the demand destination 20 and is generated in the liquefied gas storage tank 10 from the required fuel amount of the demand destination 20. When the amount of evaporative gas is large, the reliquefaction device 37 may be further operated, or the second evaporative gas compressor may be further operated. Preferably, by operating the second evaporative gas compressor first and supplying it to the customer 20, the ship speed of the ship can be increased, and the reliquefaction device 37 can be operated next. 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 the reliquefaction device 37 is further driven to efficiently process the evaporative gas continuously discharged from the liquefied gas storage tank 10 and liquefy it. There is an effect that the internal pressure of the gas storage tank 10 can be stabilized.

  As described above, the present invention has been described in detail through specific embodiments. However, this is for the purpose of specifically describing the present invention, and the present invention is not limited thereto. It will be obvious that those having ordinary knowledge in the field can make modifications and improvements.

  All simple variations and modifications of the present invention shall fall within the scope of the present invention, and the specific scope of protection of the present invention will be apparent from the appended claims.

Claims (10)

An evaporative gas supply line for connecting the liquefied gas storage tank and the high-pressure gas injection engine;
A liquefied gas supply line connecting the liquefied gas storage tank and the high pressure gas injection engine;
A pump provided on the liquefied gas supply line, pressurizing the liquefied gas stored in the liquefied gas storage tank and supplying the pressurized gas to the high-pressure gas injection engine;
A reliquefaction device for reliquefying at least part of the evaporative gas not supplied to the high-pressure gas injection engine;
A recovery line that is branched on the liquefied gas supply line and connected to the liquefied gas storage tank, and is used when the pump cools down.
A ship including a gas processing system, wherein the evaporated gas liquefied by the reliquefaction device is returned to the liquefied gas storage tank via the recovery line. A first gas-liquid separator that separates the evaporated gas reliquefied by the reliquefaction device into a gaseous state and a liquid state;
A second gas-liquid separator that separates the liquefied gas forcedly vaporized by the forced vaporizer that forcibly vaporizes the liquefied gas into a gaseous state and a liquid state;
A first return line for returning the liquid separated by the first gas-liquid separator to the liquefied gas storage tank;
A second return line for returning the liquid state of the second gas-liquid separator to the liquefied gas storage tank;
The ship including a gas processing system according to claim 1, wherein at least a part of at least one of the first return line, the second return line, or the recovery line is shared. The pump is
The ship including the gas processing system according to claim 1, wherein the ship is a high-pressure pump that pressurizes to 200 bar to 400 bar.   The marine vessel including the gas processing system according to claim 2, further comprising a bypass line connecting the second return line before the forced vaporizer.   The marine vessel including the gas processing system according to claim 4, further comprising a heterogeneous fuel power generation engine that consumes the liquefied gas or the evaporated gas stored in the liquefied gas storage tank. The first gas-liquid separator supplies the separated gas to a gas combustion device that consumes flash gas or evaporative gas, and the separated liquid is returned to the liquefied gas storage tank,
6. The gas processing according to claim 5, wherein the second gas-liquid separator supplies the separated gas to the heterogeneous fuel power generation engine, and returns the separated liquid to the liquefied gas storage tank. Ship including system.   The liquefied gas flowing inside each of the first return line and the second return line merges with each other when the high pressure gas injection engine and the heterogeneous fuel power generation engine are all driven, and the liquefied gas storage tank. A ship including the gas processing system according to claim 6. The second gas-liquid separator is
The ship including a gas processing system according to claim 7, wherein the ship is a heavy carbon separator that matches a methane number required by the heterogeneous fuel power generation engine. A recovery pump provided on the first return line for returning the liquid liquefied gas stored in the first gas-liquid separator to the liquefied gas storage tank;
A detour line for detouring the recovery pump,
The liquid liquefied gas stored in the first gas-liquid separator bypasses the recovery pump via the bypass line when the internal pressure of the first gas-liquid separator is equal to or higher than a preset pressure value. Supplied to the liquefied gas storage tank,
3. The gas processing system according to claim 2, wherein when the internal pressure of the first gas-liquid separator is less than a preset pressure value, the first gas-liquid separator is supplied to the liquefied gas storage tank via the recovery pump. Ship. The preset pressure value is
The ship including the gas processing system according to claim 9, which is 5 bar to 6 bar.

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