KR101857325B1 - A Treatment System of Liquefied Gas - Google Patents

Abstract

A liquefied gas processing system according to an embodiment of the present invention includes a fuel supply device for processing a liquefied gas or an evaporated gas supplied from a liquefied gas storage tank to a customer; And a gas burning device for burning the liquefied gas or the evaporated gas supplied from the liquefied gas storage tank or the fuel supply device to improve the exhaust temperature transferred to the purifier.
The liquefied gas processing system according to the present invention has an effect that the exhaust gas supplied to the SCR can be heated by the gas combustion device to realize the optimized function of the SCR, and the fuel of the gas combustion device can be supplied , It is effective to improve the energy efficiency of the ship, to satisfy the IMO Tier Ⅲ regulation and the fuel mileage manufacturing index, and to prevent waste of fuel.

Description

Description of the Related Art A Treatment System of Liquefied Gas

The present invention relates to a liquefied gas processing 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.

These liquefied gases are supplied to various customers and used. Recently, LNG carrier that uses LNG as fuel for LNG carriers that transport liquefied natural gas has been developed. The method used is applied to ships other than LNG carriers.

However, the temperature and pressure of the liquefied gas required by the customer such as the engine may be different from the state of the liquefied gas stored in the liquefied gas storage tank. Therefore, recently, research and development have been conducted on technologies for controlling the temperature and pressure of the liquefied gas stored in a liquid state to supply it to a customer.

In addition, the International Maritime Organization (IMO) has recently enacted a regulation to strengthen the ship's nitrogen oxide emission regulations (IMO Tier III, for example), EEDI (Energy Efficiency Design Index) And regulations are being enforced, and there are strict regulations on emission of pollutants and energy efficiency of ships.

Accordingly, a lot of research and development have been carried out in order to satisfy the above-mentioned requirements and improve the energy efficiency of ships when manufacturing each ship.

An object of the present invention is to provide a liquefied gas processing system for supplying a fuel gas supplied to an engine of a gas combustion apparatus for heating an exhaust gas supplied to an SCR.

A liquefied gas processing system according to an embodiment of the present invention includes a fuel supply device for processing a liquefied gas or an evaporated gas supplied from a liquefied gas storage tank to a customer; And a gas burning device for burning the liquefied gas or the evaporated gas supplied from the liquefied gas storage tank or the fuel supply device to improve the exhaust temperature transferred to the purifier.

Specifically, the gas combustion apparatus may be supplied with the liquefied gas or the evaporation gas in a mixed state, and the purifier may be an SCR (Selective Catalytic Reduction).

Specifically, the fuel supply device includes: a liquefied gas processing device that pressurizes the liquefied gas stored in the liquefied gas storage tank, vaporizes the liquefied gas through a vaporizer, and supplies the vaporized gas to the customer; And an evaporative gas processing device for pressurizing the evaporative gas generated in the liquefied gas storage tank to an evaporator gas compressor and supplying the evaporated gas to the customer, wherein the gas combustion device is a liquefied gas processing device, Gas or evaporative gas may be supplied and burned.

Specifically, the evaporative gas compressor is composed of a plurality of stages and is multi-stage pressurized, and the gas combustion apparatus can supply and discharge the evaporative gas branched from at least one of the stages of the evaporative gas compressor.

Specifically, the gas combustion device may be supplied with the liquefied gas pressurized by the pump and burn it.

Specifically, an evaporative gas liquefier for expanding or depressurizing the evaporated gas pressurized in the evaporative gas compressor to at least partially liquefy the evaporated gas; A first gas-liquid separator for separating a liquid and a gaseous gas from an evaporation gas which has passed through the evaporation gas liquefier; And an evaporation gas heat exchanger for recovering the cold heat of the evaporation gas supplied from the liquefied gas storage tank and the cold gas of the gas supplied from the first gas-liquid separator, The combustion apparatus can burn and burn at least a part of the gas supplied from the first gas-liquid separator.

Specifically, the apparatus further includes a nitrogen regulator for separating nitrogen by supplying at least a portion of the gaseous gas supplied from the first gas-liquid separator, wherein the gas combustion apparatus receives at least a portion of the gaseous gas supplied from the nitrogen regulator It can burn.

Specifically, the liquefied gas processing apparatus includes a temporary storage tank provided between the liquefied gas storage tank and the pump, and the gas combustion apparatus may further include a temporary storage tank for storing the evaporated gas generated in the temporary storage tank, have.

Specifically, a forced vaporizer for supplying and vaporizing the liquefied gas stored in the liquefied gas storage tank; And a second gas-liquid separator for receiving liquefied gas from the forced vaporizer to remove heavy carbon (HHC) and supplying a liquefied gas having a high methane content to the customer, wherein the gas- The second gas-liquid separator can supply and supply the liquefied gas having a high methane content to the customer.

Specifically, the apparatus may further include a waste heat recovery device driven by the heat source supplied from the purifier.

Specifically, the waste heat recovery apparatus includes: an economizer for generating steam using the heat source; A turbine generating a rotational force by using the steam supplied from the economizer; A generator for generating electric power using a rotational force generated in the turbine; And a condenser for condensing the steam discharged from the turbine.

The liquefied gas processing system according to the present invention has an effect that the exhaust gas supplied to the SCR can be heated by the gas combustion device to realize the optimized function of the SCR, and the fuel of the gas combustion device can be supplied , It is effective to improve the energy efficiency of the ship, to satisfy the IMO Tier Ⅲ regulation and the fuel mileage manufacturing index, and to prevent waste of fuel.

1 is a conceptual diagram of a liquefied gas processing system according to a first embodiment of the present invention.
2 is a conceptual diagram of a liquefied gas processing system according to a second embodiment of the present invention.
3 is a conceptual diagram of a liquefied gas processing system according to a third embodiment of the present invention.
4 is a conceptual diagram of a liquefied gas processing system according to a fourth embodiment of the present invention.
5 is a WHRS conceptual diagram of a liquefied gas processing system according to an embodiment of the present invention.

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

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

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

1, the liquefied 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 processing apparatus 30, (40), a gas combustion device (50), and a purifier (60).

Hereinafter, the liquefied gas may be used to encompass all gaseous fuels generally stored in a liquid state, such as LNG or LPG, ethylene, ammonia, etc. In the case where the gas is not in a liquid state by heating or pressurization, . This also applies to the evaporative gas. In addition, LNG can be used to mean not only NG (Natural Gas) in liquid state but also NG in supercritical state for convenience, and evaporation gas can be used to include not only gaseous evaporation gas but also liquefied evaporation gas And the gas gas may be a flash gas.

The liquefied gas storage tank (10) stores liquefied gas to be supplied to the customer (20). The liquefied gas storage tank 10 must store the liquefied gas in a liquid state, wherein the liquefied gas storage tank 10 may have the form of a pressure tank.

In the liquefied gas storage tank 10, the internal pressure may be increased as the liquefied gas stored therein is evaporated to generate the evaporation gas, and the internal pressure may be designed to withstand the internal pressure.

The customer 20 uses the evaporated gas and the liquefied gas supplied from the liquefied gas storage tank 10 as fuel. At this time, the customer 20 may be a high-pressure gas injection engine (for example, MEGI).

As the piston (not shown) inside the cylinder (not shown) reciprocates by the combustion of the liquefied gas, the engine rotates the crankshaft (not shown) connected to the piston and the shaft Can be rotated. Therefore, as the propeller (not shown) connected to the shaft rotates when the consumer 20 is driven, the hull can move forward or backward.

Of course, in this embodiment, the customer 20 may be an engine for driving the propeller, but it may be an engine for generating power or an engine for generating other power. In other words, 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 customer 20 is supplied with the evaporated gas and the flash gas pressurized by the evaporative gas compressor 31 to be described later to obtain the driving force. The state of the evaporative gas and the flash gas supplied to the consumer 20 may vary depending on the state required by the consumer 20.

The consumer 20 may include a high-pressure consumer 21 and a low-pressure consumer 22. [

The high-pressure consumer 21 is a customer 21 using a high-pressure evaporation gas of about 300 bar, for example, can be an MEGI engine, can use evaporative gas supplied from the liquefied gas storage tank 10, And a heated liquefied gas may be used.

The high pressure consumer 21 may be a dual fuel engine (DF engine) capable of dual fuel use. A dual-fuel engine is a two-stroke DF engine, typically 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, the ignition fuel uses HFO (Heavy Fuel Oil) or MDO (Marine Diesel Oil), the ratio of the ignition fuel to the high-pressure gas is about 5:95, and the injection amount of the ignition fuel is adjusted to 5 to 100% It is possible. 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 low-pressure consumer 22 is a consumer 20 using low-pressure evaporation gas of about 7 to 10 bar, for example, a DFDE engine. Further, the low-pressure consumer 22 is a dual-fuel engine that can use dual fuel, and can use oil as fuel as well as liquefied gas. Here, the low-pressure consumer 22 can be driven by receiving the evaporative gas branched and discharged from the intermediate stage of the evaporative gas compressor 31 to be described later.

The table for each engine for pressure, combustion temperature, stroke, RPM, and fuel mixture is described below for the customer (20).

<Pressure> High pressure Low pressure MEGI XDF, DFDE, DFDG

&Lt; Combustion Temperature (Whether Nox Occurred) > High temperature (low Nox reduction rate) Low temperature (high Nox reduction rate) MEGI (Oil, LNG), XDF (Oil), DFDE (Oil), DFDG (Oil) XDF (LNG), DFDE (LNG), DFDG (LNG)

<Administration> Two-stroke Four-stroke MEGI, XDF DFDE, DFDG

<RPM> Medium speed engine Low-speed engine DFDE, DFDG MEGI, XDF

The customer 20 may be a 2sDF engine or a 4sDF engine and may be discharged after the exhaust or waste heat source is used through the turbocharger 201 provided in each engine. In this case, the exhaust gas discharged directly from each engine, that is, the waste heat source, can have a temperature of about 3 to 400 degrees with high-temperature and high-pressure exhaust. Such high-temperature and high-pressure exhaust drives the turbocharger 201, And can have a temperature of about 240 to 270 degrees. Here, the exhaust, that is, the waste heat source can be supplied to the purifier 60 to be described later through the waste heat source supply line 202.

The 2sDF engine has a high combustion temperature, which is very high during compression and may cause Nox (nitrogen oxides) in the exhaust. 4sDF engine has low combustion temperature due to low combustion, so it can not generate NOx in exhaust through premixed combustion, but when it is burned with oil, NOx is generated in exhaust. In this case, the exhaust gas of the 4sDF engine can also pass through the purifier 60.

The NOx is classified as an important air pollutant, and is purified by the purifying unit 60 to be described later and discharged to the outside of the ship. The purifying unit 60 will be described in detail.

In the customer 20 of the present invention, as shown in the above table, NOx may be generated for each drive of the engine, and all the engines for which NOx is generated may be applied to the customer 20.

The evaporation gas processing apparatus 30 processes the evaporation gas supplied from the liquefied gas storage tank 10 to the customer 20 and can include the evaporation gas compressor 31 and the evaporation gas first line 301 .

The evaporation gas processing apparatus 30 can pressurize the evaporation gas supplied from the liquefied gas storage tank 10 in the evaporation gas compressor 31 and supply the evaporation gas to the consumer 20 through the first evaporation gas line 301.

The evaporative gas compressor (31) pressurizes the evaporative gas generated in the liquefied gas storage tank (10). The evaporation gas compressor 31 can pressurize the evaporation gas generated and discharged from the liquefied gas storage tank 10 and supply the evaporation gas to the evaporation gas heat exchanger 32 or the demander 20.

The plurality of evaporation gas compressors (31) can pressurize the evaporation gas at multiple stages. For example, five evaporation gas compressors 31 may be provided so that the evaporation gas is pressurized in five stages. The five-stage pressurized gas can be pressurized to 200 to 400 bar and supplied to the customer 20 through the first line 301 of the gas.

Between the plurality of evaporative gas compressors 31, an evaporative gas cooler (not shown) may be provided. When the evaporation gas is pressurized by the evaporation gas compressor 31, the temperature can also be raised in accordance with the pressure increase. Therefore, the present embodiment can lower the temperature of the evaporation gas again by using the evaporation gas cooler. The evaporative gas cooler may be installed in the same number as that of the evaporative gas compressor 31, and each evaporative gas cooler may be provided downstream of each evaporative gas compressor 31.

As the evaporation gas compressor 31 pressurizes the evaporation gas, the evaporation gas rises in pressure and the boiling point rises, so that the evaporation gas can be liquefied even at a relatively high temperature. Therefore, this embodiment can increase the pressure of the evaporation gas to the evaporation gas compressor 31 so that the evaporation gas can be easily liquefied.

The evaporation gas first line 301 may be provided with a valve (not shown) on the line, and the valve may control the flow rate of the evaporation gas supplied to the customer 20 through opening control.

The liquefied gas processing device 40 processes the liquefied gas supplied from the liquefied gas storage tank 10 to the customer 20 and can include a boosting pump 41, have.

The liquefied gas processing apparatus 40 supplies the liquefied gas stored in the liquefied gas storage tank 10 to the high pressure pump 42 through the boosting pump 41 and pressurizes the liquefied gas at high pressure in the high pressure pump 42 It is possible to vaporize the liquefied gas in the after-vaporizer 43 and supply it to the customer 20.

The liquefied gas processing apparatus 40 may further include a liquefied gas first line 401. The liquefied gas first line 401 may be provided with a valve (not shown) on the line, and the valve may control the flow rate of the liquefied gas through opening regulation and may be a three-way valve.

The boosting pump 41 may be provided on the liquefied gas first line 401 in a reciprocating manner or may be provided inside the liquefied gas storage tank 10 in a sleep mode and may be provided in the high pressure pump 42 The positive liquefied gas can be supplied to prevent the cavitation of the high-pressure pump 42. Further, the boosting pump 41 is capable of depressurizing the liquefied gas from the liquefied gas storage tank 10 to pressurize the liquefied gas from several to several tens of bar, preferably from 1 to 25 bar.

The high-pressure pump 42 secondarily pressurizes the liquefied gas in the liquid state, which is provided in the liquefied gas first line 401 and pressurized by the boosting pump 41, and supplies it to the vaporizer 43, which will be described later. At this time, the high-pressure pump 42 pressurizes the liquefied gas to a pressure required by the customer 20, for example, 200 to 400 bar, and supplies the liquefied gas to the customer 20 so that the customer 20 produces power through the liquefied gas .

The vaporizer 43 is provided on the liquefied gas first line 401 and exchanges the liquefied gas with the heat exchange medium. The vaporizer 43 may be provided in the liquefied gas supply line 16 between the customer 20 and the high pressure pump 42 and heat exchanges the liquefied gas supplied from the high pressure pump 42 using a heat exchange medium 20).

The vaporizer 43 can heat the liquefied gas while maintaining the pressure of 200 bar to 400 bar, which is the pressure discharged from the high-pressure pump 42, and then heat the liquefied gas in the state of 30 to 60 degrees and supply it to the customer 20.

The gas combustion apparatus 50 supplies liquefied gas or evaporated gas from the liquefied gas storage tank 10, the evaporative gas processing apparatus 30 or the liquefied gas processing apparatus 40 and burns it. Thereby raising the exhaust temperature to be delivered to the engine 60. Here, the gas combustion device 50 can be supplied with the liquefied gas or the evaporated gas mixed and burned.

The gas combustion apparatus 50 may be supplied with various fuels to increase the exhaust temperature from the customer 20 to the purifier 60 and may be used as the combustion heat. 51-53, respectively.

The gas combustion apparatus 50 may further include a gas combustion fuel first line 51, a gas combustion fuel second line 52, and a gas combustion fuel third line 53.

Each of the lines 51 to 53 may be provided with a valve (not shown) on the line, and the valve may control the flow rate of the fluid supplied to the gas combustion device 50 through opening adjustment.

The gas combustion apparatus 50 supplies the vaporized gas or the liquefied gas stored in the liquefied gas storage tank 10 via the gas combustion fuel first line 51 And can be used to generate combustion heat, and can be used to generate combustion heat by supplying an evaporative gas pressurized by the evaporative gas compressor 31 through the gas combustion fuel second line 52, Is pressurized by the high-pressure pump 42 through the line 53 and is supplied with gas vaporized by the vaporizer 43 to generate combustion heat.

The gas combustion apparatus 50 may be supplied with various fuels through the first to third lines 51 to 53 of the gas combustion fuels and may be used as combustion heat to be supplied to the purifier 60 from the customer 20 It is possible to effectively raise the exhaust temperature to be delivered.

Since the exhaust gas of the engine passes through the turbocharger 201 and the temperature of the exhaust gas is lower than the optimal temperature for the NOx to react with the catalyst, 60, whereby the purifying section 60 requires a heat of heat, and thus a heat source for heating the exhaust gas is required before the exhaust gas is supplied.

Therefore, in the embodiment of the present invention, the exhaust gas supplied to the purifier 60 is heated through the gas burner 50, and the first to third lines 51 - 53 or the excess liquefied gas is used, it is possible to prevent the waste of the fuel and to use the energy efficiently.

The purifier 60 can purify the exhaust supplied from the customer 20 in a state in which the exhaust gas is further heated by the gas combustion device 50. Here, the purifier 60 may be an SCR (Selective Catalytic Reduction), but is not limited thereto.

The purifier 60 can also purify the exhaust supplied from the customer 20 in a state where the exhaust gas is further heated by the gas combustion device 50.

In the embodiment of the present invention, the consumer 20 may be an engine, and the fuel used in such an engine is discharged with NOx (nitrogen oxides) during the combustion process. These NOx are stable N2O, NO, N2O3, NO2, N2O5 and unstable NO3. Here, those that exist to cause air pollution are NO and NO2, and these substances are usually referred to as nitrogen oxides. High concentrations of nitrogen oxides cause photochemical reactions, fogging, and secondary damage, and nitrogen oxides are classified as important air pollutants.

The influence of nitrogen oxides (typically NO2) causes smog due to photochemical decomposition, absorbs visible light, decreases visibility, and discolors or corrodes the material. In addition, plants have damage which destroys cells, discoloration of leaves, ability to reduce carbon assimilation, and has harmful effects on humans that mainly lead to toxic effects on the lungs.

In order to treat such nitrogen oxides, the purifier 60 of the embodiment of the present invention may be selective catalytic reduction (SCR).

Selective catalytic reduction (hereinafter referred to as SCR) is a method in which nitrogen oxides contained in the exhaust gas generated in the customer 20 can be used as a reducing agent (ammonia can be used as a reducing agent, but not limited to, CO, H2, Which can be converted into harmless nitrogen and water vapor and then discharged.

The purifying section 60 has a very high processing efficiency of 80% or more and has a very large effect by the denitration technique. Also, since the IMO Tier III regulation will be implemented in IMO in recent years, the purification unit 60 may be most effective to satisfy this requirement.

Further, since the purifying section 60 causes the highest reaction efficiency at a reaction temperature of approximately 300 to 400 degrees, the temperature of the additional heating furnace of the gas combustion apparatus 50 is increased to the exhaust gas discharged from the engine of the customer 20 The exhaust gas may be most suitable.

The purifier 60 according to the embodiment of the present invention further includes a nitrogen discharge line (not shown) for connecting the nitrogen demand consumer (not shown) and the purifier 60 consuming nitrogen .

Since the nitrogen oxide in the purifying section 60 is converted into nitrogen and water vapor, the nitrogen separated by the purifying section 60 can be supplied to the nitrogen demand line through the nitrogen discharge line.

Here, the nitrogen stored in the nitrogen demand site can serve as a sealing function for various machines (not shown), or the heat and sealing of the cold or liquefied gas storage tank 10 of the re-liquefying apparatus (not shown) Can be performed. Therefore, the nitrogen consumer can include the above-described devices. However, since the above-described operations can be used in ships for a variety of purposes, the nitrogen demand site requiring nitrogen is not limited to the above-described apparatuses.

The purifier 60 has an effect of preventing the exhaust gas produced in the customer 20 from being discharged to the outside and causing environmental pollution, and at the same time, can satisfy the IMO Tier III regulations. Further, the purifier 60 can produce nitrogen, which is required in a ship (not shown), through purification of exhaust gas, thereby reducing the cost of purchasing nitrogen.

As described above, the liquefied-gas treatment system 1 according to the first embodiment of the present invention is provided with the purifying section 60 to optimize the IMO Tier III regulations to be subsequently fermented by reducing the nitrogen oxides discharged through the exhaust gas to the outside There is an effect that can be done.

The liquefied gas processing system 1 according to the present invention has an effect that the exhaust gas supplied to the purifier 60 can be heated by the gas burner 50 to enable the optimized function of the purifier 60 to be realized And the combustion source for driving the gas combustion device 50 is supplied through surplus gases in the ship such as surplus flash gas and surplus evaporation gas to improve the energy efficiency of the ship and to prevent waste of fuel .

FIG. 2 is a conceptual diagram of a liquefied gas processing system according to a second embodiment of the present invention, and FIG. 5 is a WHRS conceptual diagram of a liquefied gas processing system according to an embodiment of the present invention.

2 and 5, a liquefied gas processing system 2 according to an embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, an evaporative gas processing apparatus 30, a liquefied gas A treatment device 40, a gas combustion device 50, a purifier 60, and a waste heat recovery device 70.

In this embodiment, the configurations of the liquefied gas storage tank 10 and the customer 20 are the same as or similar to those of the first embodiment. The same reference numerals are given to the same or corresponding components as those of the above-described embodiment, and a duplicate description thereof will be omitted.

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

The evaporation gas processing apparatus 30 processes the evaporation gas supplied from the liquefied gas storage tank 10 to the customer 20 and supplies the evaporated gas to the evaporation gas compressor 31, the evaporation gas heat exchanger 32, the evaporation gas liquefier 33), and a first gas-liquid separator (34).

The evaporation gas processing device 30 can pressurize the evaporation gas supplied from the liquefied gas storage tank 10 through the evaporation gas compressor 31 and supply the evaporation gas to the consumer 20, Exchanged with the evaporated gas supplied from the liquefied gas storage tank 10, and the heat-exchanged evaporated gas is decompressed or expanded through the evaporated gas liquefier 33 Liquefied vaporized gas can be separated into a gas phase and a liquid phase in the first gas-liquid separator (34).

The evaporation gas processing apparatus 30 may further include a first evaporation gas line 301, a second evaporation gas line 302, and a first gas gas line 303.

Each of the lines 301, 302, and 303 may be provided with a valve (not shown) on the line, and the valve may control the flow rate of the evaporative gas or the gaseous gas through opening regulation and may be a three-way valve.

Since the evaporation gas compressor 31 described in the first embodiment of the present invention is the same, it should be replaced.

The evaporation gas heat exchanger 32 is provided between the liquefied gas storage tank 10 and the evaporation gas compressor 31 on the evaporation gas first line 301 and is connected to the evaporation gas pressurized by the evaporation gas compressor 31 So that the evaporated gas supplied from the liquefied gas storage tank 10 can be heat-exchanged.

The evaporated gas heat-exchanged in the evaporative gas heat exchanger (32) can be supplied to the evaporative gas liquefier (33). That is, the evaporation gas heat exchanger 32 is connected to the evaporation gas compressor 31 through the evaporation gas second line 302 branched at the upstream of the consumer 20 and the evaporation gas recovered from the liquefied gas storage tank 10 to heat exchange the evaporated gas.

At this time, the evaporation gas heat exchanger (30) can cool the evaporated gas recovered along the evaporated gas second line (302) to the evaporated gas supplied from the liquefied gas storage tank (10).

The evaporation gas liquefier 33 is pressurized in the evaporation gas compressor 31 to decompress or expand the evaporated gas heat-exchanged in the evaporation gas heat exchanger 32 to liquefy at least a part thereof. For example, the evaporation gas liquefier 33 can reduce the pressure of the evaporation gas to 1 bar to 10 bar, the evaporation gas can be liquefied and reduced to 1 bar when transferred to the liquefied gas storage tank 10, The cooling effect can be achieved.

Here, the evaporated gas pressurized in the evaporated gas compressor 31 is cooled by heat exchange with the evaporated gas supplied from the liquefied gas storage tank 10 in the evaporated gas heat exchanger 32, but the pressure is discharged from the evaporated gas compressor 31 The discharge pressure can be maintained. In this embodiment, the evaporation gas is cooled by evaporating the evaporation gas using the evaporation gas liquefier 33, so that the evaporation gas can be liquefied. At this time, the greater the pressure range to be depressurized, the greater the cooling effect of the evaporative gas. For example, the evaporative gas liquefier 33 can reduce the evaporated gas pressurized to 300 bar by the evaporative gas compressor 31 to 1 bar.

The evaporation gas liquefier 33 may be a line Thompson valve. Alternatively, the evaporative gas liquefier 33 may comprise an expander (not shown). In the case of the Row Thompson valve, depressurization can effectively cool the evaporated gas so that at least some of the evaporated gas is liquefied. Here, the inflator may also be made of an expander (not shown).

On the other hand, the inflator can be driven without using any extra power, and in particular, the efficiency of the liquefied gas processing system 2 can be improved by utilizing the generated power as electric power for driving the evaporative gas compressor 31. The power transmission may be accomplished by, for example, a gear connection or an electric conversion and the like.

The first gas-liquid separator (34) separates the gas from the decompressed or expanded evaporated gas in the evaporative gas liquefier (33). In the first gas-liquid separator 34, the evaporated gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas is recovered as flash gas upstream of the evaporative gas heat exchanger 32, (Not shown).

Here, the evaporated gas supplied to the first gas-liquid separator 34 may be decompressed and cooled in the evaporative gas liquefier 33. For example, in the evaporative gas compressor 31, the evaporation gas may be multi-stage pressurized to have a pressure of 200 bar to 400 bar, and the temperature may be around 45 degrees. The evaporated gas raised to a temperature of about 45 degrees is recovered by the evaporation gas heat exchanger 32 and is heat-exchanged with the evaporation gas of about 100 degrees supplied from the liquefied gas storage tank 10, And is supplied to the evaporation gas liquefier 33. At this time, in the evaporative gas liquefier 33, the evaporated gas is cooled by the reduced pressure and can have a pressure of about 1 bar and a temperature of about -162.3 degrees.

As described above, in this embodiment, since the evaporation gas supplied to the first gas-liquid separator 34 is reduced in pressure by the evaporation gas liquefier 33 to have a temperature lower than -162 degrees, about 30 to 40% .

In this embodiment, the liquefied gas is recovered to the liquefied gas storage tank 10, and the flash gas generated in the first gas-liquid separator 34 is supplied to the evaporation gas heat exchanger (not shown) 32 and the flash gas may be supplied through the evaporative gas compressor 40 and then supplied to the customer 20 or may be supplied to the gas combustion device 50 so as to be burned.

The liquefied gas and the flash gas are supplied to the first gas line 303, the fourth gas combustion fuel line 54, and the liquefied gas return line 304, respectively, in the first gas-liquid separator 34 To the gas combustion device 50, to the upstream of the evaporative gas heat exchanger 32 on the liquefied gas first line 301 or to the liquefied gas storage tank 10.

The liquefied gas return line 304 is connected from the first gas-liquid separator 34 to the liquefied gas storage tank 10 to recover the liquefied gas to the liquefied gas storage tank 10 and the gas gas first line 303 The first gas-liquid separator 34 is connected to the front end of the evaporation gas heat exchanger 32 on the first evaporation gas line 301 to recover the flash gas. The fourth gas- Is connected to the first line (51) of the gas combustion fuel in the first line (34) to recover the flash gas to prevent the flash gas from being wasted and wasted.

In this embodiment, since the flash gas supplied from the first gas-liquid separator 34 is supplied to the gas combustion device 50, waste of the flash gas can be prevented.

The embodiment of the present invention may further include a nitrogen regulator (not shown). The nitrogen regulator can receive at least a part of the flash gas or gas gas supplied from the first gas-liquid separator 34 by the second gas gas line (not shown), separates nitrogen from the supplied gas gas, Nitrogen is supplied to a nitrogen source (not shown), and at least a portion of the nitrogen-depleted gas can be returned to the gas gas first line 303 by a third gas line (not shown) The removed gaseous gas residue can be supplied to the gas combustion device (50).

The nitrogen regulator removes nitrogen, which is an inert gas, and supplies it to the gas combustion device 50, so that the gas combustion device 50 can smoothly perform combustion.

The liquefied gas processing apparatus 40 processes the liquefied gas supplied from the liquefied gas storage tank 10 to the customer 20 and includes a boosting pump 41, a high-pressure pump 42, a vaporizer 43, (44).

The liquefied gas processing apparatus 40 supplies the liquefied gas stored in the liquefied gas storage tank 10 to the high pressure pump 42 through the boosting pump 41 and pressurizes the liquefied gas at high pressure in the high pressure pump 42 It is possible to vaporize the liquefied gas in the after-vaporizer 43 and supply it to the customer 20.

The boosting pump 41, the high-pressure pump 42 and the vaporizer 43 are the same as or similar to those described in the first embodiment of the present invention,

The gas combustion apparatus 50 supplies liquefied gas or evaporated gas from the liquefied gas storage tank 10, the evaporative gas processing apparatus 30 or the liquefied gas processing apparatus 40 and burns it. Thereby improving the exhaust temperature to be delivered to the exhaust pipe 60. Here, the gas combustion device 50 can be supplied with the liquefied gas or the evaporated gas mixed and burned.

The gas combustion apparatus 50 may be supplied with various heat sources to improve the exhaust temperature from the customer 20 to the purifier 60 and may be used as the combustion heat. 51 to 54).

The gas combustion apparatus 50 further includes a gas combustion fuel first line 51, a gas combustion fuel second line 52, a gas combustion fuel third line 53, and a gas combustion fuel fourth line 54 can do.

Each of the lines 51 to 54 may be provided with a valve (not shown) on the line, and the valve may control the flow rate of the fluid supplied to the gas combustion device 50 through opening control, Valve.

The gas combustion apparatus 50 may be used to generate combustion heat by receiving the liquefied gas stored in the liquefied gas storage tank 10 through the first line 51 of the gas combustion fuel and may be used as the gas combustion fuel second line 52 And is pressurized by the high-pressure pump 42 through the gas combustion fuel third line 53, and is supplied to the vaporizer (not shown) 43 to supply the liquefied gas and generate combustion heat.

The gas combustion device 50 may be used to generate combustion heat by receiving the flash gas separated from the first gas-liquid separator 34 through the fourth gas-combustion fuel line 54. That is, by using the flash gas generated in the course of re-liquefaction through the evaporative gas heat exchanger 32 as combustion heat, it is possible to prevent waste of fuel and to use energy efficiently.

The gas combustion apparatus 50 can be supplied with various heat sources through the first to fourth lines 51 to 54 of the gas combustion fuels and can be used as combustion heat to be supplied to the purifier 60 The exhaust temperature to be delivered can be effectively improved.

The purifier 60 can purify the exhaust supplied from the customer 20 in a state in which the exhaust gas is further heated by the gas combustion device 50. Here, the purifier 60 may be an SCR (Selective Catalytic Reduction), but is not limited thereto.

The purifier 60 can supply the heat source to the waste heat recovering device 70 after the exhaust supplied from the consumer 20 is supplied and cleaned by the gas combustion device 50 in a further heated state.

In the embodiment of the present invention, since the nitrogen oxide is converted into nitrogen and water vapor in the purifying section 60, the nitrogen separated by the purifying section 60 can be supplied to the nitrogen consumer through the nitrogen discharge line, 60 can be supplied to the waste heat recovery device 70 to be described later through the heat source supply line 601 because it contains high temperature.

The purifier 60 can produce nitrogen, which is required in a ship (not shown), through the purification of exhaust gas, thereby reducing the cost of purchasing nitrogen, The waste heat recovery device 70 can be reused such as power generation and operation of the propulsion device, so that efficient energy utilization can be achieved.

The waste heat recovery system 70 may be driven by using a heat source supplied from the purifier 60 and specifically to a purifier 60 that is purified by the purifier 60 and supplied from the gas- And can be driven by supplying the exhaust gas of the demanded consumer 20 heated by the additional heating (hereinafter, used in combination as a waste heat source).

Hereinafter, the waste heat recovery device 70 will be described in more detail with reference to FIG. 4 is a WHRS conceptual diagram of a liquefied gas processing system according to an embodiment of the present invention.

The waste heat recovery apparatus 70 may include an economizer 71, a turbine 72, a generator 721, and a condenser 73. The economizer 71 generates steam by using the waste heat source and the turbine 72 generates rotational force by using the steam supplied from the economizer 71 and the generator 721 generates the turbine 72 And the condenser 73 can condense the steam discharged from the turbine 72. The condenser 73 is a condenser for condensing the steam discharged from the turbine 72,

The waste heat recovery apparatus 70 may include a steam circulation line 701. The steam circulation line 701 may include an economizer 71, a turbine 72, and a condenser 73.

The high temperature steam purified in the purifier 60 is supplied to the economizer 71 through the heat source supply line 601 and the economizer 71 applies the additional heat source to the high temperature steam, And then supplies the water vapor to the turbine 72 through the steam circulation line 701. [ The turbine 72 is supplied with high-temperature water vapor to generate a rotational force, and the rotational force generated thereby generates electric power or generates propulsion through the generator 721. The water vapor discharged from the turbine 72 is supplied to the condenser 73 through the steam circulation line 701 and condensed in the condenser 73 to be returned to the economizer 71 through the steam circulation line 701 .

The waste heat recovery apparatus 70 can generate electric power or generate a propulsive force through the generator 721 using the heat source supplied from the purifier 60 and thus can maximize the energy consumption of the ship .

As described above, the liquefied gas processing system 2 according to the present invention includes the gas combustion device (not shown) driven to increase the heat of reaction of the purifier 60, the flash gas generated in the course of re-liquefaction through the evaporative gas heat exchanger 32 50), it is possible to prevent waste of fuel and to use energy efficiently.

The liquefied gas processing system 2 according to the present invention is provided with a WHRS 70 to burn exhaust gas and flash gas of the engine 20 and to maximize energy efficiency by using waste heat of exhaust gas And it has an effect of satisfying the EEDI, and it is possible to optimize to the IMO Tier III regulation to be subsequently fermented by reducing the nitrogen oxides discharged to the outside through the exhaust gas purification unit 60.

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

3, the liquefied gas processing system 3 according to the embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, a vaporized gas processing apparatus 30, a liquefied gas processing apparatus 40, a gas combustion device 50, a purifier 60, and a waste heat recovery device 70.

This embodiment differs from the first embodiment in that the configuration other than the evaporation gas heat exchanger 32, the first gas-liquid separator 34, the gas combustion device 50, the seventh line 57 of gas- Which is the same as or similar to the embodiment. The same reference numerals are given to the same or corresponding components as those of the above-described embodiment, and a duplicate description thereof will be omitted.

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

The evaporation gas heat exchanger 32 is provided between the liquefied gas storage tank 10 and the evaporation gas compressor 31 on the evaporation gas first line 301 and is connected to the evaporation gas pressurized by the evaporation gas compressor 31 It is possible to exchange heat between the evaporated gas supplied from the liquefied gas storage tank 10 and the flash gas separated from the first gas-liquid separator 34.

The evaporated gas heat-exchanged in the evaporative gas heat exchanger (32) may be supplied to the evaporative gas liquefier (33) or the evaporative gas compressor (31). That is, the evaporation gas heat exchanger 32 is connected to the evaporation gas compressor 31 through the evaporation gas second line 302 branched at the upstream of the consumer 20 and the evaporation gas recovered from the liquefied gas storage tank 10 to heat exchange the evaporated gas. The evaporation gas heat exchanger 32 exchanges heat between the evaporation gas pressurized by the evaporation gas compressor 31 and the evaporation gas second line 302 and the flash gas supplied through the first gas line 303, .

At this time, the evaporation gas heat exchanger 30 can cool the evaporation gas recovered along the evaporation gas second line 302 to the evaporation gas supplied from the liquefied gas storage tank 10, Can be cooled with the flash gas supplied through the gas supply line 303.

In this case, since the evaporation gas supplied to the evaporation gas liquefier 33 is cooled not only by the evaporation gas but also by the flash gas, the liquefaction efficiency due to the reduced pressure can be greatly increased.

The flash gas passing through the evaporative gas heat exchanger 32 can be discharged to the outside. Here, the flash gas may be supplied to the gas combustion device 50 for burning the fuel and burned.

The first gas-liquid separator (34) separates the gas from the decompressed or expanded evaporated gas in the evaporative gas liquefier (33). In the first gas-liquid separator 34, the evaporated gas is separated into a liquid and a gas so that the liquid is supplied to the liquefied gas storage tank 10, and the gas is recovered as flash gas upstream of the evaporative gas compressor 31, 50).

Here, the evaporated gas supplied to the first gas-liquid separator 34 may be decompressed and cooled in the evaporative gas liquefier 33. For example, in the evaporative gas compressor 31, the evaporation gas may be multi-stage pressurized to have a pressure of 200 bar to 400 bar, and the temperature may be around 45 degrees. The evaporated gas raised to a temperature of about 45 degrees is recovered by the evaporation gas heat exchanger 32 and is heat-exchanged with the evaporation gas of about 100 degrees supplied from the liquefied gas storage tank 10, And is supplied to the evaporation gas liquefier 33. At this time, in the evaporative gas liquefier 33, the evaporated gas is cooled by the reduced pressure and can have a pressure of about 1 bar and a temperature of about -162.3 degrees.

As described above, in this embodiment, since the evaporation gas supplied to the first gas-liquid separator 34 is reduced in pressure by the evaporation gas liquefier 33 to have a temperature lower than -162 degrees, about 30 to 40% .

In this embodiment, the liquefied evaporated gas is recovered to the liquefied gas storage tank 10, the flash gas generated in the first gas-liquid separator 34 is recovered to the evaporated gas first line 301 without being discarded, The gas and the flash gas may be pressurized through the evaporative gas compressor 40 and then supplied to the customer 20 or may be supplied to the gas combustion device 50 for combustion.

When the vaporized gas is separated into the liquid and the gas in the first gas-liquid separator 34, the liquefied vaporized gas and the flash gas are respectively supplied to the first gas-liquid separator 34 and the second gas-liquid separator 34 through the gas gas first line 303 and the liquefied gas return line To the combustion apparatus 50, the liquefied gas first line 301, or the liquefied gas storage tank 10.

The liquefied gas return line is connected from the first gas-liquid separator 34 to the liquefied gas storage tank 10 to recover the evaporated gas in the liquid state to the liquefied gas storage tank 10, 1 gas-liquid separator 34 to the gas-fired device 50 via the vapor-gas heat exchanger 32 or connected to the first line 301 of the vaporized gas so that the flash gas is discarded and wasted.

At this time, the gas gas first line 303 is connected to the evaporation gas heat exchanger 32 in the first gas-liquid separator 34 so that the flash gas is heat-exchanged with the evaporative gas returning through multi-stage compression through the evaporative gas compressor 31 Heat exchange with the vaporized gas supplied from the liquefied gas storage tank 10 can be performed to increase the re-liquefaction efficiency or to pre-heat the liquefied gas.

At this time, the flash gas may be cooled by being decompressed by the evaporation gas liquefier 33, as mentioned above, to be -162.3 degrees.

In this embodiment, the gaseous vaporized gas in the vaporized gas cooled through the vaporized gas liquefier 33 is separated into flash gas in the first gas-liquid separator 34 and supplied to the vaporized gas heat exchanger 32, The liquefaction efficiency of the evaporation gas can be increased to 60% or more by sufficiently lowering the temperature of the evaporation gas recovered from the gas compressor 31 to the evaporation gas heat exchanger 32 and the evaporation gas liquefier 33. [

In this embodiment, since the flash gas supplied from the first gas-liquid separator 34 is supplied to the gas combustion device 50 via the evaporative gas heat exchanger 32, waste of the flash gas can be prevented.

The gas combustion apparatus 50 is constructed such that the gas combustion fuel fourth line 54 is eliminated and the gas combustion fuel seventh line 57 is added to the liquefied gas processing system 2 according to the second embodiment of the present invention, Which is different from the gas combustion device 50 in Fig.

The gas combustion apparatus 50 can be used for generating combustion heat by receiving the flash gas separated from the first gas-liquid separator 34 through the seventh line 57 of the gas combustion fuel. That is, by using the flash gas generated in the course of re-liquefaction through the evaporative gas heat exchanger 32 as combustion heat, it is possible to prevent waste of fuel and to use energy efficiently.

As described above, the liquefied gas processing system 3 according to the present invention includes the gas combustion apparatus (not shown) driven to increase the heat of reaction of the purifier 60, the flash gas generated in the process of re-liquefaction through the evaporation gas heat exchanger 32 50), it is possible to prevent waste of fuel and to use energy efficiently.

4 is a conceptual diagram of a liquefied gas processing system according to a fourth embodiment of the present invention.

4, the liquefied gas processing system 4 according to the embodiment of the present invention includes a liquefied gas storage tank 10, a customer 20, a vaporized gas processing apparatus 30, a liquefied gas processing apparatus 40, a gas combustion device 50, a purifier 60, a waste heat recovery device 70, a forced vaporizer 81, a second gas-liquid separator 82, and a second heater 83.

The configuration of this embodiment is the same as or similar to that of the first embodiment except for the liquefied gas processing device 40, the gas combustion device 50, the forced vaporizer 81, the second gas-liquid separator 82 and the second heater 83 . The same reference numerals are given to the same or corresponding components as those of the above-described embodiment, and a duplicate description thereof will be omitted.

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

The liquefied gas processing apparatus 40 supplies the liquefied gas stored in the liquefied gas storage tank 10 to the high pressure pump 42 through the boosting pump 41 and pressurizes the liquefied gas at high pressure in the high pressure pump 42 It is possible to vaporize the liquefied gas in the after-vaporizer 43 and supply it to the customer 20. A temporary storage tank (not shown) is provided between the boosting pump 41 and the high-pressure pump 42 to temporally store the liquefied gas discharged from the boosting pump 41, Can be made constant.

The boosting pump 41, the high-pressure pump 42 and the vaporizer 43 are the same as or similar to those described in the first embodiment of the present invention,

The temporary storage tank 44 is provided between the liquefied gas storage tank 10 and the high pressure pump 42, that is, between the boosting pump 41 and the high pressure pump 42, The liquefied gas to be supplied can be temporarily stored before being supplied to the high-pressure pump 42. [

The temporary storage tank 44 stores the amount of the boosting pump 41 that is larger than the amount of the supplied directly to the high-pressure pump 42, so that the flow rate supplied to the high-pressure pump 42 can be maintained constantly.

In addition, the temporary storage tank 44 may be in the form of a pressure vessel, since the liquefied gas may be vaporized during storage and evaporative gas may be generated.

In the fourth embodiment of the present invention, the first forced evacuation gas line 801 and the second forced evacuation gas line 802 may be further included.

The first forced vapor line 801 may include a forced vaporizer 81, a second gas-liquid separator 82 and a second heater 83 and may include a valve (not shown) And can control the flow rate of the evaporative gas supplied to the customer 20 through adjustment of the opening degree of the valve, and can be a three-way valve.

The second forced vapor line 802 may be provided with a valve (not shown) on the line and is connected to the evaporative gas heat exchanger 32 The flow rate can be controlled and can be a three-way valve.

At this time, the forced vaporized gas second line 802 is set such that the forcedly vaporized gas through the forced vaporizer 81 is mixed with the vaporized gas supplied from the liquefied gas storage tank 10 and the vaporized gas heat exchanger 32 Liquid separator 82 on the forced vaporized gas first line 801 so that the liquefied gas storage tank 10 on the first vaporized gas line 301 and the vaporized gas heat exchanger (32).

The forced vaporizer 81 is provided between the liquefied gas storage tank 10 and the second gas-liquid separator 82 on the first forced-vapor gas line 801, and supplies the liquefied gas stored in the liquefied gas storage tank 10 And can be forcedly vaporized.

That is, the forced vaporizer 81 is operated when the flow rate of the evaporation gas is insufficient, so that the flow rate of the evaporation gas supplied to the demander 20 can be increased.

The forced vaporizer 81 can partially vaporize the liquefied gas by adjusting the heating temperature in order to increase the methane price of the liquefied gas supplied to the customer 20. The heating temperature is in the range of about -80 to -120 degrees Lt; / RTI &gt;

The second gas-liquid separator 82 is provided between the forced vaporizer 81 and the second heater 83 on the forced-vapor gas first line 801 so that the liquefied gas is supplied from the forced vaporizer 81, (HHC) and liquefied gas of high methane can be supplied to the customer 20.

The second gas-liquid separator 82 is supplied with partially vaporized evaporation gas from the forced vaporizer 81 to liquefy the heavier carbon HHC having a relatively low liquefaction point and to supply the liquefied gas to the liquefied gas storage tank 10), and the partially vaporized liquefied gas, which has a relatively high liquefaction point and can not be liquefied, can be supplied to the customer 20.

At this time, the second gas-liquid separator 82 can supply the partial gasified liquefied gas, which has a relatively high liquefaction point and can not be liquefied, to the gas combustion device 50 through the gas combustion fuel sixth line 56.

The second heater 83 is disposed between the second vapor-liquid separator 82 and the consumer 20 on the first forced vaporizing gas line 801 and is provided between the second gas-liquid separator 82 and the high- The vaporized liquefied gas can be further heated and supplied to the customer 20.

The second heater 83 can completely vaporize the partially vaporized liquefied gas and supply it to the customer 20 and can heat the partially vaporized liquefied gas to a temperature required by the customer 20.

The gas combustion apparatus 50 is a gas combustion fuel fifth and sixth lines 55 and 56 added in the liquefied gas processing system 1 according to the first embodiment of the present invention.

The gas combustion apparatus 50 is connected to the second gas-liquid separator 82 via the gas-combustion fuel sixth line 56 via the fifth gas-fired fuel line 55 and the evaporation gas generated from the temporary storage tank 44 The separated vaporized gas or the liquefied gas containing the low methane separated from the second gas-liquid separator 82 is supplied as the combustion heat to prevent the waste of the fuel and enable the efficient use of energy.

As described above, in the liquefied-gas treatment system 4 according to the fourth embodiment of the present invention, the second gas-liquid separator 82 separates the partially vaporized liquefied gas, which has a relatively high liquefaction point and is not liquefied, As the combustion heat of the gas combustion device 50 driven to raise the temperature of the combustion gas, it is possible to prevent the waste of the fuel and to use the energy efficiently.

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: Liquefied gas treatment system 10: Liquefied gas storage tank
20: Demand point 201: Turbocharger
202: waste heat source supply line of customer 30: evaporation gas processing device
301: Evaporative gas first line 302: Evaporative gas second line
303: gas gas first line 304: liquefied gas return line
31: Evaporative gas compressor 32: Evaporative gas heat exchanger
33: evaporation gas liquefier 34: first gas-liquid separator
40: liquefied gas processing device 401: liquefied gas first line
41: booster pump 42: high pressure pump
43: vaporizer 44: temporary storage tank
50: gas combustion device 51: gas combustion fuel first line
52: gas combustion fuel second line 53: gas combustion fuel third line
52: gas combustion fuel fourth line 55: gas combustion fuel fifth line
56: gas combustion fuel line 6 57: gas combustion fuel line 7
60: Purification unit 601: Heat source supply line
70: waste heat recovery device 701: steam circulation line
71: Economizer 72: Turbine
721: generator 73: condenser
801: Forced evaporation gas first line 802: Forced evaporation gas second line
81: forced vaporizer 82: second gas-liquid separator
821: Heavy carbon return line 83: Second heater

Claims (11)

A fuel supply device for treating a liquefied gas or an evaporated gas supplied from the liquefied gas storage tank to the engine;
A turbocharger driven by exhaust gas discharged from the engine;
A gas combustion device for raising the temperature of the exhaust gas discharged through the turbocharger;
An SCR which is supplied with an exhaust gas which is heated by the gas combustion apparatus and which improves a purification rate and purifies nitrogen oxides contained in the exhaust gas; And
And a waste heat recovery device driven using waste heat supplied from the SCR,
Wherein the gas-
An excess evaporation gas generated from the liquefied gas storage tank or an excess evaporation gas generated from the fuel supply device is supplied as fuel,
In the SCR,
After the nitrogen oxide is separated into nitrogen and water vapor,
The nitrogen is supplied to the nitrogen demand site and reused,
And the steam is supplied to the waste heat recovery device to supply the waste heat. The gas combustion apparatus according to claim 1,
Wherein the liquefied gas or the evaporation gas is supplied in a mixed state and combusted. 2. The fuel supply system according to claim 1,
A liquefied gas processing device that pressurizes the liquefied gas stored in the liquefied gas storage tank with a pump, vaporizes the liquefied gas through a vaporizer, and supplies the gas to the engine; And
And an evaporation gas processing device for pressurizing the evaporation gas generated in the liquefied gas storage tank with an evaporative gas compressor and supplying the pressurized gas to the engine,
Wherein the gas-
And a liquefied gas or an evaporated gas is supplied from the liquefied gas processing apparatus or the evaporated gas processing apparatus to burn the liquefied gas. 4. The evaporative gas compressor according to claim 3,
A plurality of stages, which are multi-stage pressurized,
Wherein the gas-
Wherein the evaporative gas compressor is supplied with the evaporative gas branched from at least one of the ends of the evaporative gas compressor and burns it. The gas combustion apparatus according to claim 3,
And the liquefied gas pressurized by the pump is supplied and burned. The method of claim 3,
An evaporative gas liquefier for expanding or reducing the pressure of the evaporated gas pressurized in the evaporative gas compressor to at least partially liquefy the evaporated gas;
A first gas-liquid separator for separating a liquid and a gaseous gas from an evaporation gas which has passed through the evaporation gas liquefier; And
Further comprising an evaporation gas heat exchanger for recovering the cold heat of the evaporation gas supplied from the liquefied gas storage tank and the cold gas of the gas supplied from the first gas-liquid separator,
Wherein the gas-
Wherein the first gas-liquid separator is supplied with at least a part of the gas gas and burns the gas. The method according to claim 6,
Further comprising a nitrogen regulator for separating nitrogen from at least a portion of the gaseous gas supplied from said first gas-liquid separator,
Wherein the gas-
Wherein at least a portion of the gaseous gas supplied from the nitrogen regulator is supplied and combusted. The apparatus according to claim 3, wherein the liquefied-
And a temporary storage tank provided between the liquefied gas storage tank and the pump,
Wherein the gas-
Wherein the evaporation gas generated from the temporary storage tank is supplied and burned. The method according to claim 1,
A forced vaporizer for supplying and vaporizing the liquefied gas stored in the liquefied gas storage tank; And
And a second gas-liquid separator for receiving liquefied gas from the forced vaporizer to remove heavy carbon (HHC) and supplying a liquefied gas having a high methane content to the engine,
Wherein the gas-
Wherein the second gas-liquid separator is supplied with the vaporized gas generated from the second gas-liquid separator and is burnt, or the second gas-liquid separator is supplied with the liquefied gas having a high methane charge to be supplied to the engine. delete The waste heat recovery apparatus according to claim 1,
An economizer for generating steam using the waste heat;
A turbine generating a rotational force by using the steam supplied from the economizer;
A generator for generating electric power using a rotational force generated in the turbine; And
And a condenser for condensing the steam discharged from the turbine.

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