KR20170080460A - Vessel having Gas Treatment System - Google Patents

Abstract

A ship including a gas treatment system according to an embodiment of the present invention includes an evaporative gas suction unit that mixes evaporative gas generated from a liquefied gas storage tank with a drive fluid and supplies it to a customer; And a drive fluid supply device for supplying the drive fluid to the evaporation gas suction unit, wherein the drive fluid is a fluid other than the liquefied gas or the evaporation gas stored in the liquefied gas storage tank.

Description

[0001] VESSEL Having Gas Treatment System [0002]

The present invention relates to a vessel comprising a gas treatment system.

Liquefied natural gas (Liquefied natural gas), Liquefied petroleum gas (Liquefied petroleum gas) and other liquefied gas are widely used in place of gasoline or diesel in recent technology development.

Liquefied natural gas is a liquefied natural gas obtained by refining natural gas collected from a gas field. It is a colorless and transparent liquid with almost no pollutants and high calorific value. It is an excellent fuel. On the other hand, liquefied petroleum gas is a liquid fuel made by compressing gas containing propane (C3H8) and butane (C4H10), which come from oil in oil field, at room temperature. Liquefied petroleum gas, like liquefied natural gas, is colorless and odorless and is widely used as fuel for household, business, industrial, and automotive use.

Such liquefied gas is stored in a liquefied gas storage tank installed on the ground or stored in a liquefied gas storage tank provided in a ship which is a means of transporting the ocean. The liquefied natural gas is liquefied to a volume of 1/600 The liquefaction of liquefied petroleum gas has the advantage of reducing the volume of propane to 1/260 and the content of butane to 1/230, resulting in high storage efficiency. The temperature and pressure necessary for driving the engine using such liquefied gas as fuel may be different from the state of the liquefied gas stored in the tank.

In addition, when LNG is stored in a liquid state, some LNG is vaporized and boil off gas (BOG) is generated as heat penetration occurs in the tank. Such evaporation gas may cause problems in a liquefied gas processing system. In order to solve the problem by discharging the evaporation gas to the outside (in the past, the evaporation gas was simply discharged to the outside in order to lower the tank pressure by lowering the tank pressure), the problem was solved. However, .

 In recent years, researches and developments have been actively conducted on utilization methods such as recycling the generated evaporated gas through a liquefied gas, liquefying it, and supplying it to the engine as a technique for efficiently processing the evaporated gas.

SUMMARY OF THE INVENTION The present invention has been made to improve the prior art, and it is an object of the present invention to provide a vessel including a gas treatment system that effectively supplies liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer.

A ship including a gas treatment system according to an embodiment of the present invention includes an evaporative gas suction unit that mixes evaporative gas generated from a liquefied gas storage tank with a drive fluid and supplies it to a customer; And a drive fluid supply device for supplying the drive fluid to the evaporation gas suction unit, wherein the drive fluid is a fluid other than the liquefied gas or the evaporation gas stored in the liquefied gas storage tank.

A driving fluid supply line connecting the driving fluid supply device and the evaporation gas suction unit; An evaporation gas supply line connecting the evaporation gas sucking unit to the demander and supplying the mixed fluid discharged from the evaporation gas sucking unit to the customer; And an evaporation gas suction line connecting the liquefied gas storage tank and the evaporation gas suction unit, wherein the demander is a propulsion engine, and the evaporation gas suction unit supplies the mixed fluid to the propulsion engine as it is .

Specifically, the driving fluid may be a fluid usable in the propulsion engine.

Specifically, the propulsion engine may be a low-pressure gas injection engine that mixes air and the liquefied gas or evaporated gas to generate power.

Specifically, the driving fluid may be compressed air.

Specifically, the driving fluid supply device may be an air compressor.

The controller may further include a check valve provided on the evaporation gas supply line to prevent the backflow of the mixed fluid supplied from the evaporation gas suction unit to the customer.

Specifically, the customer may be a gas turbine.

Specifically, the driving fluid may be unique to the heating medium.

Specifically, the customer may be a heterogeneous fuel engine that generates power by mixing the thermal oil and the liquefied gas or the evaporative gas.

Specifically, the driving fluid supply device includes: a heating medium oil storage tank for storing the heating medium oil; And a heat medium oil pump for supplying the heat medium oil stored in the heat medium storage tank to the evaporation gas suction unit.

Specifically, the thermal oil may be diesel oil or lubricating oil used in the heterogeneous fuel engine.

Specifically, the driving fluid may be sea water or fresh water.

Specifically, the driving fluid supply device may be a seawater pump or a fresh water pump.

Specifically, the apparatus may further include a driving fluid removing device provided on the evaporation gas supply line for removing the driving fluid.

Specifically, the driving fluid removing device includes: a condenser for condensing a mixed fluid in which evaporation gas and a driving fluid are mixed; And a separator for separating the mixed fluid condensed from the condenser into an evaporated gas and a driving fluid.

Specifically, the apparatus may further include a heater disposed between the separator and the demander on the evaporative gas supply line, for heating the evaporative gas supplied from the separator.

Specifically, the customer is a low-pressure gas injection engine that generates propulsion force on a ship; A re-liquefying device for re-liquefying the evaporated gas; And a gas combustion unit for burning the evaporation gas.

Specifically, the driving fluid may be steam.

Specifically, the driving fluid supply device may be a steam generator.

The vessel including the gas treatment system according to the present invention has an effect of effectively supplying liquefied gas and / or evaporated gas from a liquefied gas storage tank to a customer, thereby enhancing system stability and reliability.

1 is a conceptual diagram of a gas processing system according to a first embodiment of the present invention.
2 is a conceptual diagram of a gas processing system according to a second embodiment of the present invention.
3 is a conceptual diagram of a gas processing system according to a third embodiment of the present invention.
4 is a conceptual diagram of a gas processing system according to a fourth embodiment of the present invention.
5 is an enlarged view of A shown in the fourth embodiment of the present invention.
6 is a further enlarged view of A shown in the fourth embodiment of the present invention.

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

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

The liquefied gas can be referred to irrespective of the state change, such as liquid state, gas state, mixed state of liquid and gas, supercooled state, supercritical state, and the like. Further, it is apparent that the present invention is not limited to the liquefied gas to be treated, but may be a liquefied gas processing system and / or an evaporative gas processing system, and the systems of the following drawings may be applied to each other. In addition, the mixed fluid described below may be a mixed vaporized gas or a fluid containing at least a part of the liquid phase.

Further, the embodiments of the gas treatment systems 1 to 4 of the present invention may be configured in combination with each other, and additions of the respective structures may be made at intersections with each other. The gas treatment systems 1 to 4 according to embodiments of the present invention may be mounted on a hull (not shown), wherein the vessel (not shown) may be a vessel such as an LNG carrier, a container carrier, , But is not limited thereto.

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

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

1, the gas processing system 1 according to the first embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporation gas suction unit 30, a separator 41, A condenser 42, a phase separator 50, and a feeder 61.

Hereinafter, a gas processing system 1 according to a first embodiment of the present invention will be described with reference to FIG.

Prior to describing the individual configurations of the gas processing system 1 according to the first embodiment of the present invention, the basic flow paths for organically connecting the individual configurations will be described. Here, the passage is a passage through which the fluid flows, and may be a line. However, the present invention is not limited thereto.

In the first embodiment of the present invention, the first driving fluid supply line L1, the evaporation gas suction line L2, the evaporation gas supply line L3, the first return line L4, and the second return line L5, As shown in FIG. Valves (not shown) capable of adjusting the opening degree may be provided in each line, and the supply amount of the evaporation gas may be controlled according to the opening degree of each valve.

The first drive fluid supply line L1 connects the evaporation gas suction unit 30 to the drive fluid storage tank (not shown) to supply the drive fluid to the evaporation gas suction unit 30, .

The evaporation gas suction line L2 connects the liquefied gas storage tank 10 and the evaporation gas suction unit 30 to supply the evaporation gas generated in the liquefied gas storage tank 10 to the evaporation gas suction unit 30 . Here, an evaporative gas heater (not shown) for heating the evaporative gas sucked in the liquefied gas storage tank 10 may be provided on the evaporated gas suction line L2.

The evaporation gas supply line L3 is connected to the evaporation gas suction unit 30 and the consumer 20 and has a separator 41, a condenser 42 and an upper separator 50, and the liquefied gas storage tank 10 The mixed fluid of the evaporation gas and the driving fluid generated from the mixed gas can be supplied to the customer 20.

The evaporation gas supply line L3 may further include a check valve (not shown) for preventing the backflow of the mixed fluid supplied from the evaporation gas suction unit 30 to the customer 20.

Here, the check valve may be provided between the evaporation gas suction unit 30 and the separator 41 on the evaporation gas supply line L3.

The first return line L4 connects the condenser 42 to the outside (not shown), and can discharge the first driving fluid condensed in the condenser 42 to the outside. Where the exterior may be a source or tank in which the first drive fluid is present.

The second return line L5 connects the phase separator 50 to the outside and can discharge the first driving fluid or the heavy carbon separated from the phase separator 50 to the outside. Where the exterior may be a source or tank in which the first drive fluid is present.

Hereinafter, individual constitutions which are organically formed by the above-described respective lines (L1 to L4) to implement the gas processing system 1 will be described.

The liquefied gas storage tank 10 stores a liquefied gas or an evaporated gas to be supplied to the customer 20. The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, in which case the liquefied gas storage tank 10 may have the form of a pressure tank.

Here, the liquefied gas storage tank 10 is disposed inside the hull, and four liquefied gas storage tanks 10 may be formed in front of the engine room (not shown). In addition, the liquefied gas storage tank 10 is not particularly limited to various types such as a membrane-type tank or an independent tank, for example.

The customer 20 uses the liquefied gas stored in the liquefied gas storage tank 10 or the evaporative gas generated in the liquefied gas storage tank 10 as fuel and supplies the gas to the gas combustion device 21, A power generation engine 23 and a propulsion engine 24 (shown in FIG. 4).

The customer 20 needs a liquefied gas or a vaporized gas and can be driven using the raw material as the raw material. The customer 20 may be, but is not limited to, an engine (e.g., a MEGI engine as a high pressure gas injection engine) or a gas turbine. Downstream of the evaporation gas suction unit 30, an additional pressurizing device (not shown) is provided so that the consumer 20 can pressurize the power required by the power generation engine 23 or the propulsion engine 24 (shown in FIG. 4) It is of course possible to pressurize it.

As the piston (not shown) inside the cylinder (not shown) reciprocates by the combustion of the liquefied gas or the evaporative gas, the engine rotates the crankshaft (not shown) connected to the piston and is connected to the crankshaft A shaft (not shown) can be rotated.

The present embodiment does not particularly limit the kind of the consumer 20. However, the customer 20 may be an internal combustion engine that generates driving force by combustion of evaporative gas, liquefied gas, flash gas, and oil.

The gas combustion apparatus (GCU) 21 receives the evaporation gas, burns it, and burns it. The gas combustion apparatus 21 receives the evaporation gas generated from the liquefied gas storage tank 10 and supplies the evaporated gas to the liquefied gas storage tank 10 when the generation amount of the evaporated gas is greater than the throughput that can be accommodated by the consumer 20, It is possible to prevent the internal pressure of the gas storage tank 10 from rising.

The re-liquefier 22 can re-liquefy the evaporated gas supplied from the evaporation gas suction unit 30 and return it to the liquefied gas storage tank 10. Specifically, the re-liquefying device 22 re-liquefies the evaporated gas discharged from the evaporation gas suction unit 30 at 30 to 50 bar by heat exchange with the re-liquefied refrigerant to supply the re-liquefied mixed gas to the liquefied gas storage tank (10).

The re-liquefied refrigerant is an inert gas, preferably nitrogen (N2).

The power generation engine 23 is a consumer using low-pressure evaporation gas of about 30 to 50 bar. The power generation engine 23 is supplied with low-pressure evaporative gas and can convert power into electric power. For example, the power generation engine 23 may be a DFDE engine.

The power generation engine 23 is a heterogeneous fuel engine that can use a different kind of fuel. The power generation engine 23 can use not only evaporation gas but also oil as fuel. However, the evaporation gas and oil are not mixed and supplied. . This is to prevent the mixture of two materials having different combustion temperatures from being mixed, thereby preventing the efficiency of the power generation engine 23 from deteriorating.

Here, the power generation engine 23 can be driven by receiving the evaporation gas supplied from the evaporation gas suction unit 30. [ The power generation engine 23 may be a generator (e.g., DFDG), a boiler (e.g., a boiler that generates steam) as well as the DFDE engine described above that requires evaporative gas and can be driven using the raw material as the raw material , But is not limited thereto.

The evaporation gas sucking unit (30) mixes the evaporation gas generated in the liquefied gas storage tank (10) with a driving fluid to supply it to a customer. Here, the driving fluid may be a fluid other than the liquefied gas or the evaporating gas, and preferably it may be sea water. The driving fluid storage tank in which the driving fluid is stored may be a sea.

Specifically, the evaporation gas suction unit 30 receives the driving fluid supplied through the supply device 61, and sucks the evaporation gas generated in the liquefied gas storage tank 10 through the evaporation gas suction line L2 And then supply it to the customer 20.

The evaporation gas sucking unit 30 can calculate a driving fluid amount for sucking a certain amount of evaporation gas to suck a predetermined amount of evaporation gas generated in the liquefied gas storage tank 10, And can be supplied through the driving fluid supply line L1.

The evaporation gas sucking unit 30 receives seawater as a driving fluid and sucks the evaporated gas generated in the liquefied gas storage tank 10 to mix with the seawater as the driving fluid. At this time, the kinetic energy of the driving fluid is mixed The kinetic energy of the mixed fluid is converted into the kinetic energy of the whole fluid, and then the kinetic energy of the mixed fluid is again returned to the pressure as the speed of the mixed fluid at the end portion where the cross section of the nozzle (not shown) of the evaporation gas suction unit 30 is enlarged . Thus, the evaporated gas generated in the liquefied gas storage tank 10 obtains a pressure of about 2 to 3 bar.

The evaporation gas sucking unit 30 causes the pressure of the driving fluid supplied from the supply device 61 to be relatively lowered and this pressure drop is transmitted to the suction fluid (evaporation gas generated in the liquefied gas storage tank 10) The pressure of the suction fluid can be raised by a pressure of about 1 to 1.5 bar (preferably from 1.06 bar to a pressure of about 2 to 3 bar). The pressure of the suction fluid is regulated by the pressure transfer capacity (pressure drop * drive fluid flow rate) formula )

In the embodiment of the present invention, the evaporation gas suction unit 30 independently supplies the mixed gas to the gas combustion device 21, the refueling device 22, or the power generation engine 23 at a constant flow rate .

In this case, the speed at which the vessel is propelled is controlled by the liquefied gas stored in the liquefied gas storage tank 10 through the boosting pump 11 (shown in Fig. 4) and the high-pressure pump 12 (As shown in FIG. 4). That is, the boosting pump 11 and the high-pressure pump 12 are driven depending on the propulsion speed of the ship, and the evaporation gas suction unit 30 can be driven independently of the propulsion speed of the ship.

That is, in the embodiment of the present invention, the evaporation gas suction unit 30 is advantageous in that it can be independently driven without depending on the propulsion speed of the ship by using seawater other than evaporative gas or liquefied gas as the driving fluid.

In addition, in the embodiment of the present invention, the evaporation gas suction unit 30 can be independently driven without depending on the propulsion speed of the ship, so that the power generation engine 23 always outputs a constant amount of fuel The driving reliability of the power generation engine 23 can be improved and the processing of the evaporative gas generated in the liquefied gas storage tank 10 can be continuously performed so that the internal pressure of the liquefied gas storage tank 10 can be effectively Can be managed.

When the amount of evaporative gas generated in the liquefied gas storage tank 10 is larger than the amount of evaporative gas required by the power generation engine 23 in the embodiment of the present invention, At least a part of the mixed gas supplied to the gas-liquid separator 23 can be supplied to the gas-combustion device 21 or the remelting device 22. Therefore, it is possible to treat all of the evaporated gas generated in the liquefied gas storage tank 10, thereby effectively preventing the rise of the internal pressure of the liquefied gas storage tank 10.

Further, in the embodiment of the present invention, the evaporation gas sucking unit 30 uses seawater as a driving fluid, which is relatively easy to obtain as compared with liquefied gas or vaporized gas, as a driving fluid, the storage space in the vessel is remarkably improved, It is possible to maximize the profit of ship operation due to transportation, and the use of liquefied gas or evaporative gas, which is a dangerous material, is relatively reduced, thereby improving the operational safety of the system.

In addition, when the driving fluid of the evaporation gas sucking unit 30 is usually selected as the liquefied gas or the evaporated gas, the mixed fluid discharged from the ejector becomes a liquefied gas or an evaporated gas, (For example, the gas combustion device 21, the refueling device 22, or the power generation engine 23) for increasing the processing capacity Problem).

However, in the embodiment of the present invention, since the evaporated gas suction unit 30 uses the seawater as the driving fluid instead of the liquefied gas or the evaporated gas, the specific gravity occupied by the liquefied gas or the evaporated gas in the mixed fluid becomes small, , Which makes it possible to efficiently use the entire system.

When the seawater is supplied as the driving fluid, the evaporation gas sucking unit 30 can be supplied to the customer 20 mixed with the evaporative gas as the fuel.

If the sea water is supplied to the customer 20 instead of the evaporation gas, the driving efficiency may be drastically lowered or the driving may be severely interrupted, causing serious damage to the system. In addition, since seawater always contains other foreign matter (marine microorganisms or various pollutants), when the seawater is directly supplied to the customer 20, the customer 20 may be damaged or stopped.

In order to solve such a serious problem, in the embodiment of the present invention, the separator 41, the condenser 42 and the phase separator 50 are provided to remove seawater so that seawater is supplied to the driving fluid of the evaporation gas suction unit 30 And is not supplied as the fuel of the consumer 20. Here, details of the separator 41, the condenser 42 and the phase separator 50 will be described below.

The evaporation gas suction unit 30 may be an ejector, an electric actuator, or a jet pump.

The separator 41 is provided on the evaporation gas supply line L 1 and can remove the driving fluid and / or foreign matter from the mixed fluid supplied from the evaporation gas suction unit 30.

The separator 41 can be preferably a separator for removing foreign matter, and can remove impurities contained in seawater. The seawater and / or impurities removed therefrom may be discharged to the outside (or sea) through a separate line. Needless to say, the seawater can also be separated from the separator 41.

The condenser 42 is provided on the evaporation gas supply line L 1 and can condense only the driving fluid from the mixed fluid supplied from the separator 41.

The condenser 42 can condense the driving fluid by supplying the mixed fluid with the refrigerant at a temperature at which only the driving fluid can be condensed.

Here, when the driving fluid is seawater, the freezing point of the seawater is about 2 ° C to -19 ° C, so that it can freeze from the moment when it is mixed with the evaporation gas of about minus 100 ° C. However, Can be maintained.

In order to more completely remove the seawater in such a state, in the embodiment of the present invention, the condenser 42 is provided at the rear end of the separator 41 to drive the sea water to freeze through the refrigerant, Can be removed. The removed seawater may be discharged to the outside (or sea) through the first return line L4, which is a separate line.

The phase separator 50 is capable of separating the mixed fluid supplied from the condenser 42 into the evaporating gas and the driving fluid.

The phase separator 50 can finally remove the driving fluid from the mixed fluid supplied from the evaporation gas suction unit 30. The phase separator 50 can separate the liquid phase (solid phase) from the vapor phase and the separated liquid phase (or solid phase) can be discharged to the outside (or sea) through the second return line L5, which is a separate line .

In the embodiment of the present invention, a separate heater (not shown) may be provided on the evaporation gas supply line L3, and the evaporator may be provided between the phase separator 50 on the evaporation gas supply line L3 and the consumer 20 As shown in FIG.

The heater can supply the pure evaporative gas supplied from the phase separator 50 and heat it to a temperature required by the consumer 20. The temperature of the cold heat supplied from the condenser 42 can be increased and the driving efficiency of the customer 20 can be optimized.

The supply device 61 may be a seawater pump that supplies the drive fluid to the evaporation gas suction unit 30, and preferably supplies the seawater. Here, the supply device 61 may be, for example, a centrifugal pump.

As described above, the vessel including the gas treatment system 1 according to the present invention has an effect of effectively supplying liquefied gas and / or evaporated gas from the liquefied gas storage tank 10 to the customer 20 to enhance system stability and reliability have.

2 is a conceptual diagram of a gas processing system according to a second embodiment of the present invention.

2, the gas processing system 2 according to the second embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporation gas suction unit 30, a condenser 42, A phase separator 50, a supply device 61, and a driving fluid storage tank 62. [

In this embodiment, the configuration of the driving fluid storage tank 62 is added, the separator 41 is omitted, the driving fluid is changed to steam or the heating medium flow path, and the other configurations are the same as or similar to those of the first embodiment . The same or corresponding elements as those of the first embodiment described above are denoted by the same reference numerals, and redundant description thereof will be omitted.

Hereinafter, the gas processing system 2 according to the second embodiment of the present invention will be described with reference to FIG.

In the present embodiment, a return line L6, a second driving fluid supply line L7, and a driving fluid storage tank 62 may be further provided.

The return line L6 is connected to the first return line L4 and the second return line L5 so that the driving fluid separated in the condenser 42 and / or the phase separator 50 is supplied to the driving fluid storage tank 62 ).

The second driving fluid supply line L7 connects the driving fluid storage tank 62 and the evaporation gas suction unit 30 to supply the driving fluid to the evaporation gas suction unit 30 and has a supply device 61 can do.

The supply device 61 may be a compressor for compressing the gas or a pump for pressurizing the liquid.

The supply device 61 can supply the steam or the heat medium oil supplied from the drive fluid storage tank 62 to the high pressure and supply it to the evaporation gas suction unit 30.

The driving fluid storage tank 62 stores a driving fluid for driving the evaporation gas suction unit 30 and can be connected to the second driving fluid supply line L7 and the return line L6, Can be discharged to the second drive fluid supply line L7.

The driving fluid storage tank 62 is supplied with the steam or the heat medium oil returned from the condenser 42 or the phase separator 50 where the steam or the heat medium oil is cooled by the evaporation gas to be liquid or solid. And a heating device (not shown) for heating. At this time, the heating device may be formed outside the driving fluid storage tank 62 and disposed between the supplying device 61 on the second driving fluid supply line L7 and the driving fluid storage tank 62.

In the second embodiment of the present invention, steam or heat medium oil can be used instead of seawater as a driving fluid, unlike in the first embodiment.

In the second embodiment of the present invention, the separator 41 (shown in Fig. 1) may be omitted, unlike the first embodiment. In the case of using seawater, various kinds of foreign substances are included in addition to moisture including other salts, and a separator 41 for removing the seawater is required. In the second embodiment of the present invention, however, steam or heat medium oil So that it is not necessary to remove the foreign substance, so that the separator 41 can be omitted.

Therefore, in the second embodiment of the present invention, the system construction cost is reduced, and the entire system can be efficiently used.

The evaporation gas sucking unit 30 can supply the high pressure steam or the heat medium oil from the supply device 61 and suck the evaporation gas from the liquefied gas storage tank 10 and can supply the evaporation gas and the steam And the mixture is supplied to the condenser 42 (the condenser may be a scrubber if the driving fluid is a heating medium).

The evaporation gas sucking unit 30 can suck the evaporation gas in an amount corresponding to 1/10 of the amount of the high-pressure steam supplied, and can mix the steam and the evaporation gas and discharge the mixture at a pressure of 10 to 15 bar. Here, since the thermal oil is a liquid phase, a larger amount of heat is required than in the case of steam, and this amount can be reversely calculated by the pressure transfer capacity formula as described in the first embodiment.

When the driving fluid is seawater or steam, the driving fluid is mixed with the cryogenic gas at a very low temperature (approximately minus 100 degrees Celsius), so that even a slight design error may cause a problem of freezing. This causes extreme damage to the customer 20 when supplied to the customer 20 as it is, and may also cause serious problems such as breakage in the evaporative gas suction device 30 as well.

On the other hand, when the drive fluid is used as a heat carrier oil (where the heat carrier oil may be, for example, oil, diesel, lubricant), it may be liquid at about minus 70 degrees , The above problems can be solved.

In this case, even if the oil is not at least partially removed from the scrubber 42 or the phase separator 50, the oil can be used in the customer 20, so that there is no driving problem. In this case, the supply device 61 may be a heat medium oil pump.

As described above, the ship including the gas treatment system 2 according to the present invention has the effect of effectively supplying the liquefied gas and / or the evaporated gas from the liquefied gas storage tank 10 to the customer 20 to enhance the system stability and reliability have.

3 is a conceptual diagram of a gas processing system according to a third embodiment of the present invention.

3, the gas processing system 3 according to the third embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporation gas suction unit 30, and a supply device 61 ).

In this embodiment, the separator 41, the condenser 42, the phase separator 50, the first and second return lines L4 and L5 are omitted, the driving fluid is changed to air, And is configured to be the same as or similar to the first and second embodiments. The same or corresponding elements as those of the first and second embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, a gas processing system 3 according to a third embodiment of the present invention will be described with reference to FIG.

In the third embodiment of the present invention, unlike in the first and second embodiments, sea water or steam may be used as the driving fluid, or compressed air may be used instead of the heating medium. That is, the compressed air, which is a gas as a driving fluid, is supplied to the evaporation gas suction unit 30, and the evaporated gas, which is a sucked gas, is mixed and supplied to the customer 20. Here, the supply device 61 may be an air compressor.

As compared with the first embodiment of the present invention, since the driving fluid is used as a gas, the rear-end discharge pressure of the evaporation gas suction unit 30 can be increased to 10 to 15 bar.

1 and 2) and the phase separator 50 (shown in Figs. 1 and 2) in the third embodiment of the present invention, unlike in the first and second embodiments, (Shown in Figs. 1 and 2) may be omitted.

The customer 20 is always driven by mixing the air and the evaporative gas. That is, the consumer 20 is driven by burning the evaporated gas, and in order to burn the evaporated gas, the inflow of air is necessarily required.

Accordingly, in the third embodiment of the present invention, the use of air as the driving fluid used in the evaporation gas suction unit 30 eliminates the necessity of providing a separate driving fluid removing device, The mixed fluid can be supplied directly to the customer 20.

Therefore, in the third embodiment of the present invention, the system construction cost is reduced, and the whole system can be efficiently used.

Here, the customer 20 in the third embodiment of the present invention may additionally include a separate device (not shown) for controlling the ratio of the air to the evaporation gas (air-fuel ratio).

As described above, the ship including the gas treatment system 3 according to the present invention has an effect of effectively supplying liquefied gas and / or evaporated gas from the liquefied gas storage tank 10 to the customer 20 to enhance system stability and reliability have.

Fig. 4 is a conceptual diagram of a gas processing system according to a fourth embodiment of the present invention, Fig. 5 is an enlarged view of A shown in a fourth embodiment of the present invention, Fig. A is a further enlargement of the figure.

4 to 6, a gas processing system 4 according to a fourth embodiment of the present invention includes a liquefied gas storage tank 10, a boosting pump 11, a high-pressure pump 12, a vaporizer (not shown) 13, a customer 20, and a vaporizing gas sucking unit 30.

In this embodiment, the separator 41, the condenser 42, the phase separator 50, the first and second return lines L4 and L5 are omitted, the driving fluid is changed to vaporized liquefied gas, The third drive fluid supply line L8 and the liquefied gas supply line L9 are additionally constructed and the other configurations are the same as those of the first to third embodiments The same or similar. The same or corresponding elements as those of the first to third embodiments described above are denoted by the same reference numerals, and a duplicate description thereof will be omitted.

Hereinafter, the gas processing system 4 according to the fourth embodiment of the present invention will be described with reference to Figs.

In the fourth embodiment of the present invention, a third drive fluid supply line L8 and a liquefied gas supply line L9 may be additionally provided. (Not shown) capable of adjusting the opening degree can be provided in each line, and the supply amount of the evaporation gas can be controlled according to the opening degree control of each valve, and the third driving fluid supply A three-way valve may be provided at a branch point to the line L8.

The third drive fluid supply line L8 branches between the vaporizer 13 and the propulsion engine 24 on the liquefied gas supply line L9 and is connected to the evaporation gas intake unit 30, The gas can be supplied to the evaporation gas sucking unit (30).

The liquefied gas supply line L9 may include a boosting pump 11, a high pressure pump 12 and a vaporizer 13 by connecting the liquefied gas storage tank 10 and the propulsion engine 24, The liquefied gas stored in the storage tank 10 can be pressurized to a high pressure and then vaporized and supplied to the propulsion engine 24.

The boosting pump 11 can first pressurize the liquefied gas stored in the liquefied gas storage tank 10 and supply it to the high pressure pump 12, which will be described later. Specifically, the boosting pump 11 is provided between the liquefied gas storage tank 10 and the high-pressure pump 12 on the liquefied gas supply line L9, and supplies the liquefied gas stored in the liquefied gas storage tank 10 to the high- It is possible to supply a sufficient amount to the pump 12 to prevent cavitation of the high-pressure pump 22.

The boosting pump 11 can extract the liquefied gas from the liquefied gas storage tank 10 and pressurize it to several to several tens of bars and the liquefied gas through the boosting pump 11 can be pressurized to 1 to 25 bar.

The liquefied gas stored in the liquefied gas storage tank 10 is in a liquid state. At this time, the boosting pump 11 may pressurize the liquefied gas discharged from the liquefied gas storage tank 10 to slightly increase the pressure and the temperature, and the liquefied gas pressurized by the boosting pump 11 may still be in a liquid state.

In the present embodiment, the booster pump 11 can supply the maximum flow rate to the high-pressure pump 12. [ The maximum flow rate refers to the flow rate at which the booster pump 11 can maximally discharge. In this case, since the liquefied gas in an amount larger than the required flow rate of the high-pressure pump 12 is transferred from the boosting pump 11 to the high-pressure pump 12, the high-pressure pump 12 can be smoothly driven.

The boosting pump 11 may be constructed in a manner of being located in the interior of the liquefied gas storage tank 10 or may be configured in a centrifugal manner at a position outside the level of the liquefied gas stored in the liquefied gas storage tank 10 .

The high-pressure pump 12 can pressurize the liquefied gas supplied from the boosting pump 11 (pressurize at a high pressure of about 200 bar to 400 bar) to the vaporizer 13 to be described later. Specifically, the high-pressure pump 12 is provided between the boosting pump 11 and the vaporizer 13 on the liquefied gas supply line L9, and is pressurized to a pressure of about 6 to 8 bar To the vaporizer 13 by secondary pressurization to a high pressure of about 200 to 400 bar.

The high pressure pump 12 can pressurize at a high pressure of about 200 to 400 bar and supply it to the propulsion engine 24 via the vaporizer 13 to supply the pressure required by the propulsion engine 24, (Not shown) to generate thrust through the liquefied gas.

The high-pressure pump 12 pressurizes the liquid-state liquefied gas discharged from the boosting pump 11 to a high pressure, and changes the phase of the liquefied gas to a supercritical state having a temperature and a pressure higher than a critical point . At this time, the temperature of the liquefied gas in the supercritical state may be minus 20 degrees or less, which is relatively higher than the critical temperature.

Alternatively, the high-pressure pump 12 can pressurize the liquefied gas in the liquid state to a super-cooled liquid state by pressurizing it at a high pressure. Here, the liquefied gas in the subcooled liquid state is a state in which the pressure of the liquefied gas is higher than the critical pressure and the temperature is lower than the critical temperature.

Specifically, the high-pressure pump 12 pressurizes the liquid-state liquefied gas discharged from the boosting pump 11 to a high pressure of 200 to 400 bar so that the temperature of the liquefied gas becomes lower than the critical temperature, Phase state to a subcooled liquid state. Here, the temperature of the liquefied gas in the subcooled liquid state may be minus 140 degrees to minus 60 degrees lower than the critical temperature.

Further, in the embodiment of the present invention, when the high-pressure pump 12 is provided in parallel so that one of the high-pressure pumps 12 malfunctions or shut down, the other high-pressure pump 12 can operate So that the liquefied gas supplied from the boosting pump 11 can be reliably and stably supplied to the propulsion engine 24.

The vaporizer 13 is provided on the liquefied gas supply line L9 and can heat the high-pressure liquefied gas discharged from the high-pressure pump 12. Specifically, the vaporizer 13 is provided on the liquefied gas supply line L9 between the propulsion engine 24 and the high-pressure pump 12, and heats the high-pressure liquefied gas supplied from the high-pressure pump 12, 24 can be supplied in a desired state.

That is, the vaporizer 13 heats the liquefied gas in the subcooled liquid state or the supercritical state while maintaining the pressure of 200 bar to 400 bar, which is discharged from the high-pressure pump 12, And can supply it to the propulsion engine 24 after conversion.

At this time, the vaporizer 13 can use Glycol Water, Sea Water, Steam, or engine exhaust gas as the heat for heating the liquefied gas, and the pressure of the high-pressure liquefied gas And can be supplied to the propulsion engine 24 without any change.

In the fourth embodiment of the present invention, the evaporation gas sucking unit 30 is configured such that the vaporized liquefied gas heated by the high pressure in the vaporizer 13 is supplied as driving fluid through the high-pressure pump 12 to the vaporizer 13, The evaporated gas generated in the liquefied gas storage tank 10 may be sucked through the evaporated gas suction line L2 and then supplied to the propulsion engine 24. [

Here, the evaporation gas suction unit 30 can calculate the amount of the driving fluid for sucking a certain amount of the evaporation gas to suck a predetermined amount of the evaporation gas generated in the liquefied gas storage tank 10, Can be supplied through the third driving fluid supply line L8.

The evaporation gas sucking unit 30 receives the gaseous liquefied gas as the driving fluid and sucks the evaporated gas generated in the liquefied gas storage tank 10 to mix with the gaseous liquefied gas as the driving fluid, The kinetic energy is converted into the kinetic energy of the mixed fluid as a whole. Subsequently, as the velocity of the mixed fluid at the end portion of the nozzle (not shown) of the evaporation gas suction unit 30 is enlarged, The kinetic energy is again converted into pressure. As a result, the evaporated gas generated in the liquefied gas storage tank 10 has a pressure of about 30 to 50 bar (preferably about 40 bar).

In the present invention, the driving fluid after the pressure of the liquefied gas supplied from the vaporizer 13 reaches a pressure of about 200 to 400 bar (preferably about 300 bar) or the vaporized gas sucking unit 30, The pressure of the suction fluid is increased by a pressure of about 30 to 50 bar (preferably about 40 bar) by supplying a pressure transfer capacity, which is a driving fluid flow rate, to the suction fluid (evaporation gas generated in the liquefied gas storage tank 10) .

Here, since the pressure of the driving fluid is high, the pressure of the suction fluid can be easily raised even with a small amount of fluid.

In the embodiment of the present invention, the evaporation gas suction device 30 is supplied from the high-pressure pump 12 and the vaporizer 13 at a pressure of 200 to 400 bar to supply the vaporized liquefied gas (the propulsion engine 24) The gas is supplied from the booster pump 11 and the vaporizer 13 at a pressure of 17 to 25 bar so as to be supplied with the vaporized liquefied gas and the vaporized gas stored in the liquefied gas storage tank 10 (In this case, the propulsion engine 24 may be a low-speed two-stroke low-pressure gas injection engine (XDF), and the high-pressure pump 12 may not be provided). In this case, Except for the high pressure pump 12 and the corresponding pressure, all of the components are the same as those described above, so that detailed description thereof will be omitted.

In the fourth embodiment of the present invention, the customer 20 may further include a propelling engine 24. [

The propulsion engine 24 requires a liquefied gas or an evaporating gas, and can be driven using the raw material as the raw material. Propulsion engine 24 may be, but is not limited to, an engine (e.g., a MEGI engine as a high pressure gas injection engine or an XDF engine as a low velocity two stroke low pressure gas injection engine) or a gas turbine.

Here, the propulsion engine 24 may be connected to the liquefied gas storage tank 10 through the liquefied gas supply line L9, and may be supplied with the liquefied gas or the evaporated gas pressurized at a high pressure of about 200 to 400 bar. The propulsion engine 24 can use pressurized heated or liquefied gas through the boosting pump 11, the high pressure pump 12 and the vaporizer 13 and can be used for high pressure And may be an engine for directly rotating a propeller shaft (not shown) to drive a propeller (not shown) or an engine for generating other power.

As the piston (not shown) inside the cylinder (not shown) reciprocates by the combustion of the liquefied gas or the evaporative gas, the engine rotates the crankshaft (not shown) connected to the piston and is connected to the crankshaft A shaft (not shown) can be rotated. Therefore, as the propeller connected to the propeller shaft rotates when the propulsion engine 24 is driven, the ship can move forward or backward.

Of course, in this embodiment, the propulsion engine 24 may be an engine for driving the propeller, but it may be an engine for generating power or an engine for generating other power. That is, the present embodiment does not particularly limit the kind of the propulsion engine 24. [ However, the propulsion engine 24 may be an internal combustion engine that generates driving force by combustion of evaporative gas, liquefied gas, flash gas, and oil.

The propulsion engine 24 may be a DF engine in which a heterogeneous fuel can be used. A heterogeneous fuel engine is a two-stroke DF engine, usually driven by a diesel cycle. In this diesel cycle, air is compressed by the piston, the compressed high-temperature air is ignited by a pilot fuel, and the remaining high-pressure gas is injected and exploded.

In this case, HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil) is used as the ignition fuel, and the ratio of the ignition fuel to the high-pressure gas is about 5:95, and the injection amount of the ignition fuel can be adjusted from 5 to 100% Do. Therefore, the ignition fuel is also usable as the driving fuel for the engine.

That is, when the injection amount of the ignition fuel is about 5%, evaporative gas (or heated liquefied gas; about 95%) is mainly used as the engine driving fuel, and when the injection amount of the ignition fuel is 100% Fuel (oil) is all used.

At this time, when the injection amount of the ignition fuel is about 50% (and about 50% of the evaporation gas), the ignition fuel and the evaporation gas are mixed and not ignited into the engine, but the ignition fuel is ignited first to generate a calorific value, Gas is introduced and exploded to produce a calorific value, thereby producing a calorific value required for driving the engine.

The propulsion engine 24 may also be a low speed two stroke low pressure gas injection engine (XDF). The propulsion engine 24 may be connected to the liquefied gas storage tank 10 through the liquefied gas supply line L9 and may be supplied with the liquefied gas or the evaporated gas pressurized at a low pressure of about 25 to 40 bar. The propulsion engine 24 may be a pressurized evaporated or liquefied gas through the boosting pump 11 and the vaporizer 13 and may be a low pressure engine using a low pressure vapor of about 40 bar, An engine for rotating the propeller drive shaft S3 directly to drive the propeller shaft P or an engine for generating other power.

The low-speed two-stroke low-pressure gas injection engine in the embodiment of the present invention may be a 2s DF engine (XDF engine) developed by wartsila, and may be driven according to an Otto cycle.

That is, in the low-speed two-stroke low-pressure gas injection engine, the air-fuel mixture supplied to the cylinder is first compressed to the top dead center, and at the moment when ignition is performed by the pilot fuel from the outside at the compression top dead center, So that explosive power is generated. At this time, the air-fuel mixture mass ratio may be in the form of a Lean burn engine which may be in a lean state less than 14.7: 1.

In this case, HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil) is used as the ignition fuel, and the ratio of the ignition fuel to the high-pressure gas is about 1:99.

The low-speed two-stroke low-pressure gas injection engine can generate power by supplying the liquefied gas from 25 to 40 bar, and the state of the supplied ethane can be changed depending on the state required by the low-speed two-stroke low-pressure gas injection engine.

The MEGI engine requires a high pressure of about 200 bar to about 300 bar and a power consumption of about 210 KW to about 220 KW (about 215 KW) The low pressure gas injection engine has the effect of reducing the power consumption by about 13 KW to about 17 KW (about 15 KW) for driving at a low pressure of 25 to 40 bar, have.

In addition, the MEGI engine has a disadvantage in that the driving pressure is so high that the gas processing system that accompanies it is very complicated and takes up a lot of space in order to generate the pressure required by the MEGI engine. On the other hand, the low-speed two-stroke low-pressure gas injection engine is advantageous in that the fuel supply system is very simple and the space occupied by the low-pressure gas injection engine is low because the driving pressure is low.

In the embodiment of the present invention, the propulsion engine drive shaft S1 is mechanically coupled to the power generation engine drive shaft S2 so that the propulsion engine drive shaft S1 can receive the shaft drive force from the power generation engine 23 in the embodiment of the present invention.

5, in the embodiment of the present invention, the power generation engine 23 includes a power generation engine drive shaft S2 and a second transmission device T2, and the propulsion engine 24 includes a propulsion engine drive shaft S1, A propeller drive shaft S3 and a first transmission device T1. Here, the propeller drive shaft S3 may have a propeller P at one end and may be connected to the first transmission device T1 at the other end to transmit the power generated from the propulsion engine 24 to the propeller P. [

The first transmitting device T1 may be a first gear and the second transmitting device T2 may be a second gear and the first gear T1 may be meshed with the second gear T2 .

When the amount of the evaporated gas generated in the liquefied gas storage tank 10 is larger than the amount of evaporated gas that can be consumed in the propulsion engine 24, the power generation engine 23 generates the surplus evaporated gas as the third drive fluid The evaporation gas is supplied from the evaporation gas suction unit 30 driven and supplied through the supply line L8 to be consumed to rotate the power generation engine drive shaft S2.

Here, the power generated by rotation from the power generating engine drive shaft S2 is at least partially transmitted to the first transmitting device T1 by the second transmitting device T2 and is transmitted to the first transmitting device T1 The power can be transmitted to the propeller drive shaft S3 together with the power generated in the propulsion engine 24 and transmitted to the propulsion engine drive shaft S1.

Therefore, in the fourth embodiment of the present invention, the energy consumed through the surplus evaporation gas can be assisted with the power for propelling the ship, and the use of the evaporation gas can be optimized.

6, in the embodiment of the present invention, the power generation engine 23 includes a motor (not shown) connected to the propulsion engine 24 without the propulsion engine drive shaft S1 being mechanically coupled to the power generation engine drive shaft S2 25).

The motor 25 is supplied with electric power produced by the power generation engine 23 and produces power, and may include a driving gear T11.

At this time, the propulsion engine 24 may be provided with a driven gear T12 which is engaged with a driving gear T11 provided in the motor 25. The driven gear T12 transmits power from the driving gear T11 To the propulsion engine drive shaft S1, and finally to the propeller drive shaft S1.

As described above, the vessel including the gas treatment system 4 according to the present invention has an effect of effectively supplying liquefied gas and / or evaporated gas from the liquefied gas storage tank 10 to the customer 20 to enhance system stability and reliability have.

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

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

1, 2, 3, 4: Gas treatment system 10: Liquefied gas storage tank
11: boosting pump 12: high pressure pump
13: carburetor 20: customer
21: Gas Combustion Device 22: Liquefaction Device
23: power generation engine 24: propulsion engine
25: motor 30: evaporation gas suction unit
41: separator 42: condenser
50: phase separator 61: feeder
62: Driving fluid storage tank
L1: first driving fluid supply line L2: evaporation gas suction line
L3: evaporation gas supply line L4: first return line
L5: second return line L6: return line
L7: second drive fluid supply line L8: third drive fluid supply line
L9: Liquefied gas supply line P: Propeller
S1: Propulsion engine shaft S2: Power generator shaft
S3: drive shaft T1: first transmission device
T2: second transmission device T11: drive gear
T12: driven gear

Claims (20)

An evaporative gas suction unit for mixing evaporative gas generated in the liquefied gas storage tank with a driving fluid and supplying the mixture to a customer; And
And a drive fluid supply device for supplying the drive fluid to the evaporation gas suction unit,
Wherein the drive fluid
Wherein the liquefied gas is a liquefied gas stored in the liquefied gas storage tank or a fluid other than the evaporated gas. The method according to claim 1,
A driving fluid supply line connecting the driving fluid supply device and the evaporation gas suction unit;
An evaporation gas supply line connecting the evaporation gas sucking unit to the demander and supplying the mixed fluid discharged from the evaporation gas sucking unit to the customer; And
Further comprising an evaporation gas suction line connecting the liquefied gas storage tank and the evaporation gas suction unit,
The customer is a propulsion engine,
Wherein the evaporating gas suction unit supplies the mixed fluid to the propulsion engine as it is. 3. The apparatus according to claim 2,
Wherein the fluid is usable in the propulsion engine. 4. The apparatus of claim 3, wherein the propulsion engine
Pressure gas injection engine for combusting air and the liquefied gas or evaporating gas to generate power. 2. The fuel cell system according to claim 1,
Wherein the compressed air is compressed air. 6. The apparatus according to claim 5,
Characterized in that it is an air compressor (Air Compressor). The method according to claim 1,
Further comprising a check valve provided on the evaporation gas supply line for preventing backflow of the mixed fluid supplied from the evaporation gas suction unit to the customer. The system according to claim 1,
Wherein the gas turbine is a gas turbine. 2. The fuel cell system according to claim 1,
Characterized in that it is a heat transfer fluid. 10. The system according to claim 9,
Wherein the engine is a heterogeneous fuel engine that generates power by mixing and burning the thermal oil and the liquefied or evaporated gas. 10. The apparatus according to claim 9,
A heating medium oil storage tank for storing the heating medium oil; And
And a heat medium oil pump for supplying the heat medium oil stored in the heat medium storage tank to the evaporation gas suction unit. 10. The method according to claim 9,
Characterized in that it is a diesel oil or a lubricating oil used in said heterogeneous fuel engine. 2. The fuel cell system according to claim 1,
Characterized in that it is a sea water or fresh water. 14. The apparatus according to claim 13,
Wherein the water treatment system is a seawater pump or a fresh water pump. 14. The method of claim 13,
Further comprising a drive fluid removal device disposed on the evaporation gas supply line for removing the drive fluid. 16. The apparatus according to claim 15,
A condenser for condensing the mixed fluid in which the evaporation gas and the driving fluid are mixed; And
And a separator for separating the mixed fluid condensed from the condenser into an evaporated gas and a driving fluid. 17. The method of claim 16,
Further comprising a heater disposed between the separator and the demander on the evaporation gas supply line for heating the evaporation gas supplied from the separator. The system according to claim 1,
A low pressure gas injection engine for generating propulsion force on the ship;
A re-liquefying device for re-liquefying the evaporated gas; And
And a gas combustion unit for burning the evaporation gas. 2. The fuel cell system according to claim 1,
Characterized in that the gas treatment system is a steam turbine. 20. The apparatus according to claim 19,
Wherein the steam generator is a steam generator.

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