WO2015130122A1 - 증발가스 처리 시스템 - Google Patents
증발가스 처리 시스템 Download PDFInfo
- Publication number
- WO2015130122A1 WO2015130122A1 PCT/KR2015/001916 KR2015001916W WO2015130122A1 WO 2015130122 A1 WO2015130122 A1 WO 2015130122A1 KR 2015001916 W KR2015001916 W KR 2015001916W WO 2015130122 A1 WO2015130122 A1 WO 2015130122A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- gas
- boil
- engine
- storage tank
- fuel
- Prior art date
Links
- 239000007789 gas Substances 0.000 claims abstract description 305
- 239000003949 liquefied natural gas Substances 0.000 claims abstract description 136
- 239000007788 liquid Substances 0.000 claims abstract description 68
- 239000000446 fuel Substances 0.000 claims description 67
- 230000006835 compression Effects 0.000 claims description 22
- 238000007906 compression Methods 0.000 claims description 22
- 238000000034 method Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 10
- 238000000926 separation method Methods 0.000 claims description 9
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 128
- 239000003345 natural gas Substances 0.000 description 37
- 239000002737 fuel gas Substances 0.000 description 35
- 238000002347 injection Methods 0.000 description 24
- 239000007924 injection Substances 0.000 description 24
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 15
- 239000003507 refrigerant Substances 0.000 description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 238000010586 diagram Methods 0.000 description 10
- 229930195733 hydrocarbon Natural products 0.000 description 9
- 150000002430 hydrocarbons Chemical class 0.000 description 9
- 239000004215 Carbon black (E152) Substances 0.000 description 8
- 238000001704 evaporation Methods 0.000 description 7
- 230000008020 evaporation Effects 0.000 description 7
- 239000006200 vaporizer Substances 0.000 description 7
- 239000000969 carrier Substances 0.000 description 6
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 238000009434 installation Methods 0.000 description 5
- 238000005057 refrigeration Methods 0.000 description 5
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 4
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000002485 combustion reaction Methods 0.000 description 4
- 238000007599 discharging Methods 0.000 description 4
- 229910052815 sulfur oxide Inorganic materials 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- 230000004888 barrier function Effects 0.000 description 3
- 230000009977 dual effect Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 239000003921 oil Substances 0.000 description 3
- 230000008569 process Effects 0.000 description 3
- 238000009834 vaporization Methods 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 239000001273 butane Substances 0.000 description 2
- 229910002092 carbon dioxide Inorganic materials 0.000 description 2
- 239000001569 carbon dioxide Substances 0.000 description 2
- 230000003247 decreasing effect Effects 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 238000010248 power generation Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 150000003464 sulfur compounds Chemical class 0.000 description 2
- XTQHKBHJIVJGKJ-UHFFFAOYSA-N sulfur monoxide Chemical class S=O XTQHKBHJIVJGKJ-UHFFFAOYSA-N 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- 230000006837 decompression Effects 0.000 description 1
- 239000002283 diesel fuel Substances 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000000295 fuel oil Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000009413 insulation Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 230000008520 organization Effects 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 230000002265 prevention Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 230000008439 repair process Effects 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
- F17C7/02—Discharging liquefied gases
- F17C7/04—Discharging liquefied gases with change of state, e.g. vaporisation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
- F02M—SUPPLYING COMBUSTION ENGINES IN GENERAL WITH COMBUSTIBLE MIXTURES OR CONSTITUENTS THEREOF
- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0203—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels characterised by the type of gaseous fuel
- F02M21/0215—Mixtures of gaseous fuels; Natural gas; Biogas; Mine gas; Landfill gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F02M21/00—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form
- F02M21/02—Apparatus for supplying engines with non-liquid fuels, e.g. gaseous fuels stored in liquid form for gaseous fuels
- F02M21/0218—Details on the gaseous fuel supply system, e.g. tanks, valves, pipes, pumps, rails, injectors or mixers
- F02M21/0221—Fuel storage reservoirs, e.g. cryogenic tanks
- F02M21/0224—Secondary gaseous fuel storages
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F02M21/0287—Details on the gaseous fuel supply system, e.g. tanks, valves, pipes, pumps, rails, injectors or mixers characterised by the transition from liquid to gaseous phase ; Injection in liquid phase; Cooling and low temperature storage
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
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- F25J1/0025—Boil-off gases "BOG" from storages
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
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- F25J1/0229—Integration with a unit for using hydrocarbons, e.g. consuming hydrocarbons as feed stock
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
- F25J1/0275—Construction and layout of liquefaction equipments, e.g. valves, machines adapted for special use of the liquefaction unit, e.g. portable or transportable devices
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- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
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- B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
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- B63J2099/003—Burning of transported goods, e.g. fuel, boil-off or refuse of cargo oil or fuel, or of boil-off gases, e.g. for propulsive purposes
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T10/00—Road transport of goods or passengers
- Y02T10/10—Internal combustion engine [ICE] based vehicles
- Y02T10/30—Use of alternative fuels, e.g. biofuels
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T70/00—Maritime or waterways transport
- Y02T70/50—Measures to reduce greenhouse gas emissions related to the propulsion system
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02T—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO TRANSPORTATION
- Y02T90/00—Enabling technologies or technologies with a potential or indirect contribution to GHG emissions mitigation
- Y02T90/40—Application of hydrogen technology to transportation, e.g. using fuel cells
Definitions
- the present invention relates to a boil-off gas treatment system, and more particularly, a compressor for compressing boil-off gas generated in a LNG storage tank of a ship or a floating structure, and cooled by heat exchange with the boil-off gas to be introduced into the compressor A heat exchanger, an expansion means for adiabatic expansion of the boil-off gas cooled in the heat exchanger, and a gas-liquid separator for separating the boil-off gas insulated from the expansion means and supplying liquefied natural gas to the LNG storage tank.
- the present invention relates to an evaporative gas treatment system capable of diversifying the system operation by configuring a bypass line to supply the adiabatic expanded boiled gas from the downstream of the expansion means to the downstream of the gas-liquid separator.
- Liquefied Natural Gas (hereinafter referred to as "LNG”) is a colorless and transparent liquid obtained by liquefying natural gas containing methane as its main component at about -162 °C. It has a volume of about / 600. Therefore, when liquefied and transported with LNG when transporting natural gas, it can be transported very efficiently.
- LNG Liquefied Natural Gas
- an LNG carrier that can transport (transport) LNG to sea is used.
- BOG is a kind of LNG loss, which is an important problem in the transportation efficiency of LNG, and if boil-off gas accumulates in the LNG storage tank, the pressure in the LNG storage tank may be excessively increased and the tank may be damaged.
- Various ways to deal with this have been studied.
- the gas combustion unit inevitably burns the excess BOG to control the pressure of the storage tank when there is no other way to use the BOG, resulting in a waste of chemical energy of the BOG by combustion.
- the boil-off gas generated in the LNG storage tank can be used as the fuel of the DF engine to process the boil-off gas.
- the boil-off gas may be sent to a gas combustor for incineration to protect the LNG storage tank.
- the cryogenic LNG is very sensitive to changes in the external environment such as temperature, and a considerable amount of BOG (Boil Off Gas) is generated because it continuously vaporizes in the cargo hold even during the operation of the vessel. Excessive BOG inside the storage container may cause the container to withstand the internal pressure due to an increase in the pressure inside the container, which may cause the container to explode. do. Even if the vessel is insulated, the amount of BOG generated in the storage vessel is about 0.05 vol% / day, and 4 to 6 tons per hour (t) of conventional LNG carriers, It is known that about 300 tons of liquefied natural gas is evaporated once operated.
- BOG Bit Off Gas
- a method of discharging the boil-off gas inside the storage tank to the outside of the storage tank and re-liquefying it through a re-liquefaction apparatus including a refrigerating cycle is used, wherein the boil-off gas is a refrigerant cooled to low temperature, for example After liquefaction through heat exchange with nitrogen, mixed refrigerant, etc., it is returned to the storage tank.
- the reliquefaction apparatus through such a refrigeration cycle has a problem in that the overall system control is complicated and a lot of power is consumed due to the complexity of operation.
- the present invention is to solve this problem, to provide a system that can efficiently handle the boil-off gas generated in the LNG storage tank of the ship or floating structure.
- the compressor for compressing the boil-off gas generated in the LNG storage tank of the ship or floating structure
- a gas-liquid separator for separating the evaporated gas adiabaticly expanded by the expansion means and for supplying liquefied natural gas to the LNG storage tank;
- An evaporation gas treatment system includes a bypass line for supplying the boil-off gas adiabaticly expanded from downstream of the expansion means to the downstream of the gas-liquid separator.
- a recirculation line for introducing the evaporated gas in the gas phase separated by the gas-liquid separator into the flow of the boil-off gas to be introduced into the heat exchanger from the LNG storage tank, and provided in the recirculation line and cooled in the heat exchanger.
- the apparatus may further include a cooler configured to further cool the boil-off gas to the boil-off gas separated from the gas-liquid separator.
- the apparatus may further include a first separation valve provided upstream of the gas-liquid separator and a second separation valve provided in the bypass line.
- the compressor is a multi-stage compressor in which a compression cylinder and an intermediate cooler are alternately provided, and the boil-off gas compressed through a part of the multi-stage compressor is supplied as fuel to a first engine.
- the boil-off gas compressed through the multi-stage compressor is supplied as fuel to a second engine, and the boil-off gas supplied to the first and second engines is liquefied through the heat exchanger and expansion means. Can be stored in the LNG storage tank.
- the first engine is a DF engine that can be supplied with the fuel gas boiled compressed to 5 to 20 bar
- the second engine can be supplied with fuel boiled gas boiled to 150 to 400 bar It may be a ME-GI engine.
- the expansion means may be any one of an expansion valve (J-T valve) and an expander (expander).
- the fuel supply line for compressing the boil-off gas generated in the LNG storage tank of the vessel or floating structure to supply to the engine of the vessel or floating structure;
- a gas-liquid separator separating the adiabatic expanded boil-off gas and supplying liquefied natural gas to the LNG storage tank;
- a boil-off gas treatment system including a bypass line branching from the liquefied line and adiabaticly expanded boil-off gas to bypass the gas-liquid separator to the LNG storage tank.
- a recirculation line for reintroducing the vaporized gaseous gas separated by the gas-liquid separator into the fuel supply line, and an intersection point of the recirculation line and the liquefaction line are provided, and
- the apparatus may further include a cooler configured to further cool the boil-off gas cooled by heat exchange with the boil-off gas separated from the gas-liquid separator.
- the system of the present invention is a system capable of compressing the boil-off gas generated in the LNG storage tank to supply the engine fuel, the remaining boil-off gas to re-liquefy using the cooling heat of the boil-off gas itself, does not require a separate refrigerant system Therefore, the initial installation cost burden and the equipment scale can be reduced, and the maintenance is also convenient.
- this system can reduce the operating cost of the device for reliquefaction by not installing a reliquefaction device that consumes a lot of energy for reliquefaction, and can reduce the amount of natural gas wasted by combustion in the GCU through effective reliquefaction. It can increase economics.
- the system can bypass the gas-liquid separator and bypass the gas-liquid separator to introduce into the LNG storage tank to liquefy the evaporated gas in the flash gas state by the cooling heat inside the tank. Can diversify operations
- FIG. 1 is a schematic configuration diagram of a boil-off gas treatment system according to a first embodiment of the present invention.
- FIG. 2 is a schematic diagram of a boil-off gas treatment system according to a second preferred embodiment of the present invention.
- FIG 3 is a schematic configuration diagram of a state in which the boil-off gas treatment system according to the first embodiment of the present invention is used together with the fuel gas supply system.
- FIG. 4 is a schematic configuration diagram of a boil-off gas processing system according to a third preferred embodiment of the present invention.
- FIG. 5 is a schematic diagram of a boil-off gas treatment system according to a fourth preferred embodiment of the present invention.
- FIG. 6 is a schematic diagram of a boil-off gas treatment system according to a fifth preferred embodiment of the present invention.
- FIG. 7 is a schematic configuration diagram of a boil-off gas treatment system according to a sixth preferred embodiment of the present invention.
- MEGI engines are in the spotlight as next generation eco-friendly engines that can reduce pollutant emissions by 23%, carbon dioxide by 80%, and sulfur compounds by 95% compared to diesel engines of the same class.
- Such a MEGI engine is a vessel such as an LNG carrier for storing and transporting LNG in a cryogenic storage tank.
- natural gas is used as a fuel, and a high pressure gas supply pressure of about 150 to 400 bara (absolute pressure) is required for the engine depending on the load.
- the MEGI engine can be used directly on the propellers for propulsion, for which the MEGI engine consists of a two-stroke engine rotating at low speed. That is, the MEGI engine is a low speed two-stroke high pressure natural gas injection engine.
- a DF engine for example, DFDG; Dual Fuel Diesel Generator
- DFDG Dual Fuel Diesel Generator
- the DF engine can mix and burn oil and natural gas, or use only one selected from oil and natural gas as fuel.There is less sulfur compound in the fuel than if only oil is used as fuel. little.
- the DF engine does not need to supply fuel gas at the same high pressure as the MEGI engine, and compresses the fuel gas to about several to several tens of bara.
- the DF engine drives the generator by the driving force of the engine to obtain electric power, and uses this electric power to drive the propulsion motor or to drive various devices and facilities.
- the methane component having a relatively low liquefaction temperature is evaporated preferentially.
- the methane content is high and can be supplied as a fuel to the DF engine as it is.
- the methane content is relatively lower than the methane value required by the DF engine, and the ratio of hydrocarbon components (methane, ethane, propane, butane, etc.) constituting the LNG varies depending on the region, it is vaporized as it is. Not suitable for fueling DF engines.
- the forced gasification of liquefied natural gas, and then lower the temperature can be removed by liquefying the heavy hydrocarbon (HHC; heavy hydrocarbon) component higher than the methane. After the methane is adjusted, the methane can be further heated to meet the temperature requirements of the engine.
- HHC heavy hydrocarbon
- FIG. 1 shows a schematic configuration diagram of a boil-off gas treatment system according to a first preferred embodiment of the present invention.
- boil-off gas treatment system of the present invention is applied to a high-pressure natural gas injection engine that can use natural gas as a fuel, that is, an LNG carrier equipped with a MEGI engine, but the boil-off gas treatment system of the present invention is liquefied. It can be applied to all kinds of ships equipped with gas storage tanks, such as LNG carriers, LNG RVs, etc., as well as offshore plants such as LNG FPSO, LNG FSRU.
- the boil-off gas NBOG generated and discharged from the storage tank 11 storing the liquefied gas is transferred along the boil-off gas supply line L1. It is compressed in the compressor 13 and then supplied to a high pressure natural gas injection engine, such as a MEGI engine.
- the boil-off gas is compressed by a compressor 13 to a high pressure of about 150 to 400 bara and then supplied as fuel to a high pressure natural gas injection engine, for example, a MEGI engine.
- Storage tanks are equipped with sealed and insulated barriers to store liquefied gases, such as LNG, in cryogenic conditions, but they cannot completely block heat from the outside. Accordingly, the liquefied gas is continuously evaporated in the storage tank 11, and the evaporated gas is discharged through the evaporated gas discharge line L1 to maintain the pressure of the evaporated gas at an appropriate level. Let's do it.
- a discharge pump 12 is installed inside the storage tank 11, to discharge the LNG to the outside of the storage tank if necessary.
- the compressor 13 may include one or more compression cylinders 14 and one or more intermediate coolers 15 for cooling the boil-off gas which has risen in temperature while being compressed.
- the compressor 13 may be configured to compress, for example, the boil-off gas to about 301 bara.
- FIG. 1 a compressor 13 of multistage compression including five compression cylinders 14 and five intermediate coolers 15 is illustrated, but the number of compression cylinders and intermediate coolers may be changed as necessary.
- it may be changed to have a structure in which a plurality of compressors are connected in series.
- the boil-off gas compressed by the compressor 13 is supplied to the high-pressure natural gas injection engine through the boil-off gas supply line L1, and all of the boil-off gas compressed according to the required amount of fuel required by the high-pressure natural gas injection engine
- the gas injection engine may be supplied, or only a part of the compressed boil-off gas may be supplied to the high pressure natural gas injection engine.
- the boil-off gas discharged from the storage tank 11 and compressed in the compressor 13 (that is, the entire boil-off gas discharged from the storage tank) is called a first stream
- evaporation is performed.
- the first stream of gas may be divided into a second stream and a third stream after compression so that the second stream is supplied as fuel to the high pressure natural gas injection engine and the third stream is liquefied and returned to the storage tank.
- the second stream is supplied to the high pressure natural gas injection engine through the boil-off gas supply line (L1), the third stream is returned to the storage tank (11) through the boil-off gas return line (L3).
- a heat exchanger 21 is installed in the boil-off gas return line L3 to liquefy the third stream of compressed boil-off gas. The heat exchanger 21 exchanges the third stream of compressed boil-off gas with the first stream of boil-off gas supplied to the compressor 13 after being discharged from the storage tank 11.
- the third stream of compressed boil-off gas can be liquefied by receiving cold heat from the first stream of boil-off gas before compression.
- the heat exchanger 21 heats the cryogenic evaporation gas immediately after being discharged from the storage tank 11 and the high-pressure evaporated gas compressed by the compressor 13 to liquefy the high-pressure evaporated gas.
- the boil-off gas LBOG liquefied in the heat exchanger 21 is reduced in pressure while passing through the expansion valve 22 and supplied to the gas-liquid separator 23 in a gas-liquid mixed state. While passing through the expansion valve 22, LBOG can be reduced to approximately atmospheric pressure.
- the liquefied boil-off gas is separated from the gas and the liquid component in the gas-liquid separator 23, so that the liquid component, that is, LNG, is transferred to the storage tank 11 through the boil-off gas return line L3. It is discharged from the storage tank 11 through the boil-off gas recirculation line (L5) and joined to the boil-off gas supplied to the compressor (13). More specifically, the boil-off gas recirculation line L5 extends from the top of the gas-liquid separator 23 and is connected to the upstream side of the heat-exchanger 21 in the boil-off gas supply line L1.
- the heat exchanger 21 is installed in the boil-off gas return line L3 for convenience of description, but the heat exchanger 21 actually includes a first stream of boil-off gas being transferred through the boil-off gas supply line L1. Since the heat exchange is performed between the third streams of the boil-off gas being transferred through the boil-off gas return line (L3), the heat exchanger 21 is also installed in the boil-off gas supply line (L1).
- Another expansion valve 24 may be further installed in the boil-off gas recirculation line L5 so that the gas component discharged from the gas-liquid separator 23 may be reduced in pressure while passing through the expansion valve 24.
- the third stream of boil-off gas supplied to the gas-liquid separator 23 after being liquefied in the heat exchanger 21 and the gas-component separated from the gas-liquid separator 23 are transferred to the boil-off gas recycle line L5 to exchange heat.
- a cooler 25 is installed in the boil-off gas recirculation line L5 to further cool the three streams. That is, the cooler 25 further cools the boil-off gas in the high pressure liquid state with the natural gas in the low pressure cryogenic gas state.
- the cooler 25 has been described as being installed in the boil-off gas recirculation line L5. However, in the cooler 25, the third stream of the boil-off gas being transferred through the boil-off gas return line L3 and evaporated. Since heat exchange is performed between the gas components being conveyed through the gas recirculation line (L5), the cooler 25 is also installed in the boil-off gas return line (L3).
- the compressor 13 is compressed or compressed step by step.
- the boil-off gas on the way is branched through the boil-off gas branch lines L7 and L8 and used in the boil-off gas consumption means.
- a GCU a DF Generator (DFDG), a gas turbine, or the like, which can use natural gas at a lower pressure as a fuel than a MEGI engine, may be used.
- DFDG DF Generator
- the boil-off gas generated when the cargo of the LNG carrier i.e., LNG
- the boil-off gas generated when the cargo of the LNG carrier is transported is used as the fuel of the engine or re-liquefied. Since it can be returned to the storage tank and stored, it is possible to reduce or eliminate the amount of evaporated gas consumed by the GCU, and to re-liquefy the evaporated gas without installing a reliquefaction device using a separate refrigerant such as nitrogen. Can be processed.
- boil-off gas treatment system and treatment method according to the first embodiment of the present invention there is no need to install a re-liquefaction apparatus (that is, nitrogen refrigerant refrigeration cycle, mixed refrigerant refrigeration cycle, etc.) using a separate refrigerant, There is no need to install additional equipment for supplying and storing refrigerant, which reduces the initial installation and operating costs for the entire system.
- a re-liquefaction apparatus that is, nitrogen refrigerant refrigeration cycle, mixed refrigerant refrigeration cycle, etc.
- FIG. 2 is a schematic structural diagram of a boil-off gas treatment system according to a second preferred embodiment of the present invention.
- the boil-off gas treatment system according to the second embodiment is configured to forcibly vaporize and use LNG when the boil-off gas required by the MEGI engine or the DF Generator is larger than the amount of boil-off gas naturally occurring. It is different from the boil-off gas treatment system of the first embodiment. Hereinafter, the difference from the boil-off gas treatment system of the first embodiment will be described in more detail.
- the boil-off gas NBOG generated and discharged from the storage tank 11 storing the liquefied gas is transferred along the boil-off gas supply line L1.
- a high-pressure natural gas injection engine such as a MEGI engine after being compressed in the compressor 13, or to a DF generator during multistage compression in the compressor 13 to be used as fuel.
- a high-pressure natural gas injection engine such as a MEGI engine after being compressed in the compressor 13, or to a DF generator during multistage compression in the compressor 13 to be used as fuel.
- the storage tank when the amount of boil-off gas as fuel required by the high pressure natural gas injection engine and the DF engine is larger than the amount of boil-off gas naturally occurring in the storage tank 11, the storage tank The forced vaporization line L11 is provided so that the LNG stored in 11 can be vaporized in the forced vaporizer 31 and supplied to the compressor 13.
- the amount of LNG stored in the storage tank is small so that the amount of generated evaporation gas is small or the amount of evaporated gas as fuel required by various engines is naturally Even if the amount of generated boil-off gas is greater than that, the fuel can be stably supplied.
- FIG. 3 is a schematic configuration diagram showing a state in which the boil-off gas treatment system according to the present invention is used together with a fuel gas supply system for supplying fuel to an engine.
- FIG. 3 shows a state in which the boil-off gas treatment system according to the first embodiment of the present invention shown in FIG. 1 is coupled with a fuel gas supply system, the boil-off gas treatment system according to the second embodiment provides fuel gas.
- the boil-off gas treatment system according to the second embodiment provides fuel gas.
- it can be used in combination with the system.
- the ship fuel gas supply system of the present invention shown in FIG. 3 includes a high pressure natural gas injection engine, for example, a MEGI engine, as a main engine, and a DF engine (DFDG) as a sub engine.
- a high pressure natural gas injection engine for example, a MEGI engine
- DFDG DF engine
- the main engine is used for propulsion for the operation of the ship
- the sub-engine is used for power generation to supply power to various devices and equipment installed inside the ship
- the present invention is used by the use of the main engine and the sub-engine It is not limited.
- a plurality of main engines and sub engines may be installed.
- the marine fuel gas supply system is a natural gas (ie, gaseous BOG and liquid) contained in the storage tank 11 for engines (ie, the main engine MEGI engine and the secondary engine DF engine). LNG can be supplied as a fuel.
- natural gas ie, gaseous BOG and liquid
- LNG can be supplied as a fuel.
- the fuel gas supply system of the present invention includes a main BOG supply line L1 as an evaporation gas supply line for supplying the main engine with a BOG housed in the storage tank 11, And a BOG sub supply line L8 branching from the BOG main supply line L1 to supply the BOG to the sub engine.
- the BOG main supply line L1 has the same configuration as the boil-off gas supply line L1 in FIGS. 1 and 2, but in the description made with reference to FIG. 3, the BOG main supply line (ie, the BOG sub-supply for the DF engine) In order to distinguish it from the line L8), it is called BOG main supply line L1.
- the fuel gas supply system of the present invention includes an LNG main supply line L23 for supplying LNG contained in the storage tank 11 to the main engine, and the LNG main supply.
- LNG sub-supply line (L24) for branching from the supply line (L23) to supply LNG to the secondary engine.
- the compressor 13 for compressing the BOG is installed in the BOG main supply line (L1)
- the high pressure pump 43 for compressing the LNG is installed in the LNG main supply line (L23).
- the boil-off gas (NBOG) generated in the storage tank 11 storing the liquefied gas and discharged through the BOG discharge valve 41 is transferred along the main BOG supply line L1 and compressed in the compressor 13, and then pressurized.
- Natural gas injection engines such as MEGI engines.
- the boil-off gas is compressed to a high pressure of about 150 to 400 bara by the compressor 13 and then supplied to the high pressure natural gas injection engine.
- Storage tanks are equipped with sealed and insulated barriers to store liquefied gases, such as LNG, in cryogenic conditions, but they cannot completely block heat from the outside. Accordingly, the liquefied gas is continuously evaporated in the storage tank 11, and the evaporated gas is discharged inside the storage tank 11 to maintain the pressure of the evaporated gas at an appropriate level.
- liquefied gases such as LNG, in cryogenic conditions
- the compressor 13 may include one or more compression cylinders 14 and one or more intermediate coolers 15 for cooling the boil-off gas which has risen in temperature while being compressed.
- the compressor 13 may be configured to compress, for example, the boil-off gas to about 301 bara.
- FIG. 1 a compressor 13 of multistage compression including five compression cylinders 14 and five intermediate coolers 15 is illustrated, but the number of compression cylinders and intermediate coolers may be changed as necessary.
- it may be changed to have a structure in which a plurality of compressors are connected in series.
- the boil-off gas compressed by the compressor 13 is supplied to the high-pressure natural gas injection engine through the main BOG supply line L1, and all of the compressed boil-off gas is compressed according to the required amount of fuel required by the high-pressure natural gas injection engine.
- the gas injection engine may be supplied, or only a part of the compressed boil-off gas may be supplied to the high pressure natural gas injection engine.
- the sub BOG supply line L8 for supplying fuel gas to the sub engine DF engine is branched from the main BOG supply line L1. More specifically, the secondary BOG supply line L8 is branched from the main BOG supply line L1 so as to branch off the boil-off gas in the middle of being multistage-compressed in the compressor 13.
- FIG. 1 shows that the two-stage compressed BOG is branched and a part thereof is supplied to the sub engine through the sub BOG supply line L8.
- the DF engine which is a sub engine, lowers the BOG pressure and then reconnects to the sub engine when branching off the BOG under high pressure from the rear end of the compressor (13). It can be inefficient because it must be supplied.
- the methane component having a relatively low liquefaction temperature is preferentially vaporized, the methane content in the case of boiled gas can be supplied as a fuel to the DF engine as it is. Therefore, the BOG main supply line and the BOG sub supply line do not need to be installed separately for methane value control.
- the boil-off gas compressed or compressed in the compressor 13 can be branched through the boil-off gas branch line L7 to be used by the BOG consumption means.
- the evaporation gas consumption means a GCU, a gas turbine, or the like, which can use natural gas at a lower pressure than fuel as a MEGI engine, can be used.
- the boil-off gas branch line L7 is preferably branched from the BOG sub-supply line L8, as shown in FIG.
- the process of returning is the same as that already described above with reference to FIGS. 1 and 2, and thus a detailed description thereof will be omitted.
- a discharge pump 12 installed inside the storage tank 11 for discharging the LNG to the outside of the storage tank 11, and is primarily compressed by the discharge pump 12.
- the high pressure pump 43 for secondaryly compressing the LNG to the pressure required by the MEGI engine is provided.
- Discharge pump 12 may be installed one inside each storage tank (11). Only one high pressure pump 43 is shown in FIG. 3, but a plurality of high pressure pumps may be connected and used in parallel as necessary.
- the pressure of the fuel gas required by the MEGI engine is a high pressure of about 150 to 400 bara (absolute pressure).
- high pressure should be considered to mean a pressure of about 150 to 400 bara (absolute pressure) required by the MEGI engine.
- the LNG discharged through the discharge pump 12 from the storage tank 11 storing the liquefied gas is transferred along the LNG main supply line L23 and supplied to the high pressure pump 43. Subsequently, the LNG is compressed to high pressure in the high pressure pump 43 and then supplied to the vaporizer 44 to be vaporized. Vaporized LNG is supplied as fuel to a high pressure natural gas injection engine, such as a MEGI engine. Since the pressure required by the MEGI engine is supercritical, LNG compressed at high pressure is neither gas nor liquid. Thus, the expression of vaporizing LNG compressed at high pressure in the vaporizer 44 should be considered to mean that the temperature of the LNG in supercritical state is raised to the temperature required by the MEGI engine.
- the sub LNG supply line L24 for supplying fuel gas to the sub engine DF engine is branched from the main LNG supply line L23. More specifically, the secondary LNG supply line L24 is branched from the primary LNG supply line L23 so as to branch off the LNG before being compressed by the high pressure pump 43.
- the vaporizer 45, the gas-liquid separator 26, and the heater 27 are installed in the secondary LNG supply line L24 to adjust the methane number and temperature of the LNG supplied as fuel to a value required by the DF engine.
- the LNG is heated in the vaporizer 45 and only partially vaporized.
- the fuel gas which is partially vaporized and mixed with a gaseous state (ie, natural gas) and a liquid state (ie, LNG), is supplied to the gas-liquid separator 46 to be separated into gas and liquid. Since the vaporization temperature of the HHC component having a high calorific value is relatively high, the proportion of the heavy hydrocarbon component is relatively high in the liquid LNG which is not vaporized in the partially vaporized fuel gas. Therefore, by separating the liquid component in the gas-liquid separator 46, that is, separating the heavy hydrocarbon component, the methane number of the fuel gas can be increased.
- the heating temperature in the vaporizer 45 can be adjusted to obtain an appropriate methane number.
- the heating temperature in the vaporizer 45 may be determined in the range of approximately -80 to -120 degrees Celsius.
- the liquid component separated from the fuel gas in the gas-liquid separator 46 is returned to the storage tank 11 through the liquid component return line L5.
- the boil-off gas return line L3 of the boil-off gas treatment system and the liquid component return line L25 of the fuel gas supply system may join and extend to the storage tank 11.
- the methane-adjusted fuel gas is supplied to the heater 47 through the LNG sub supply line L24, and further heated to a temperature required by the sub engine, and then supplied as fuel to the sub engine.
- the secondary engine is for example DFDG
- the methane number required is generally 80 or more.
- the methane value before the separation of the heavy hydrocarbon component is 71.3
- the lower heating value (LHV) is 48,872.8 kJ / kg (1). atm, saturated vapor basis).
- the methane number is 95.5
- the LHV is 49,265.6 kJ / kg.
- the fuel gas may be supplied to the engine after being compressed through the compressor 13 or may be supplied to the engine after being compressed through the high pressure pump 43.
- ships such as LNG carriers and LNG RVs are used to transport LNG from the place of production to the place of consumption. Therefore, when operating from the place of production to the place of consumption, the ship operates in the state of Laden, which is loaded with LNG in a storage tank, and unloads the LNG. After returning to the production site, the storage tanks are operated in a nearly empty ballast state. In the Leiden state, the amount of LNG is relatively high, so the amount of boil-off gas is relatively high. In the ballast state, the amount of LNG is low, so the amount of LNG is relatively low.
- the amount of boil-off gas generated when the storage tank capacity of LNG is approximately 130,000 m 3 to 350,000 m 3 is about 3 to 4 ton in Leiden. / h and about 0.3 to 0.4 ton / h in ballast.
- the amount of fuel gas required by the engines is approximately 1 to 4 ton / h (mean about 1.5 ton / h) for the MEGI engine and approximately 0.5 ton / h for the DF engine (DFDG).
- the BOR Bit Off Rate
- the amount of BOG is also decreasing.
- the compressor line i.e., L1 and L8 in FIG. 3
- the high pressure pump line i.e., L23 and L24 in FIG. 3
- a large amount of evaporated gas is generated. It is preferable to supply fuel gas to the engines through the compressor line in the laden state, and to supply the fuel gas to the engines through the high pressure pump line in a ballast state in which the amount of boil-off gas is generated.
- the energy required to compress BOG by a compressor to a high pressure of 150 to 400 bara (absolute pressure) required by MEGI engines is significantly greater than the energy required to compress liquid (LNG) by a pump. Since energy is required and compressors for compressing gases at high pressures are quite expensive and also bulky, it can be considered economical to use only high pressure pump lines without compressor lines. For example, 2MW of power is consumed to drive a set of multi-stage compressors to fuel a ME-GI engine. With a high-pressure pump, only 100kW of power is consumed.
- the multi-stage compressor does not compress the boil-off gas to the high pressure required by the ME-GI engine and It may be efficient to divert the boil-off gas through the BOG branch line L7 during compression and use it as fuel in the DF engine. That is, for example, if the boil-off gas is supplied to the DF engine only through the second stage compression cylinder of the five stage compressor, the remaining three stage compression cylinders are idle.
- the power required is 2MW.However, if only 2 stages are used and the remaining three stages are idling, the power required is 600kW and the high-pressure pump supplies fuel to the ME-GI engine. The power required is 100kW. Therefore, when the amount of BOG generated is less than the fuel required in the ME-GI engine, such as in a ballast state, it is advantageous in terms of energy efficiency that BOG consumes the entire amount in a DF engine or the like and supplies LNG as fuel through a high pressure pump.
- LNG may be forcedly supplied by the compressor while supplying BOG as fuel to the ME-GI engine through the compressor.
- the BOG is collected without being discharged until the storage tank reaches a constant pressure.
- the engine may be supplied as fuel.
- the fuel gas supply system of the present invention having one compressor line and one high-pressure pump line installed together can continue normal operation through the other supply line even if a problem occurs in one supply line, and an expensive compressor With the use of less gas, the optimal fuel gas supply method can be appropriately selected and operated according to the amount of boil-off gas, thereby reducing the initial drying cost and operating cost.
- the boil-off gas generated when the cargo of the LNG carrier is transported ie, LNG
- the fuel of the engine or re-used is used as the fuel of the engine or re-used. Since it can be liquefied and returned to the storage tank for storage, it is possible to reduce or eliminate the amount of evaporated gas consumed by the GCU, and to eliminate the need for installing a reliquefaction device using a separate refrigerant such as nitrogen. Can be reliquefied and processed.
- the present invention despite the recent trend that the capacity of the storage tank is increased, the amount of generated evaporated gas is increased and the performance of the engine is improved, and the amount of fuel required is reduced. Since it can be returned to the storage tank, it is possible to prevent the waste of boil-off gas.
- a reliquefaction apparatus using a separate refrigerant i.e., a nitrogen refrigerant refrigeration cycle or a mixed refrigerant refrigeration cycle, etc.
- a separate refrigerant i.e., a nitrogen refrigerant refrigeration cycle or a mixed refrigerant refrigeration cycle, etc.
- FIG. 4 schematically shows a boil-off gas treatment system according to a third embodiment of the present invention
- FIG. 5 schematically shows a fourth embodiment in which a cooler is added to a recycle line in the third embodiment.
- FIG. 6 schematically shows a boil-off gas treatment system of a fifth embodiment of the present invention
- FIG. 7 schematically shows a sixth embodiment in which a cooler is added to the recirculation line RL in the fifth embodiment.
- the systems for treating boil-off gas described below of the present invention can be applied to all kinds of offshore structures in which liquefied gas storage tanks are installed, ie, LNG carriers, ships such as LNG RV, and offshore plants such as LNG FPSO and LNG FSRU.
- the boil-off gas treatment system compresses the boil-off gas generated in the LNG storage tank T of the ship or the floating structure and supplies the compressed gas to the engine of the ship or the floating structure.
- LNG storage tank (T) is equipped with a sealing and insulating barrier to store the liquefied gas such as LNG in a cryogenic state, but can not completely block the heat transmitted from the outside. Accordingly, the liquefied gas is continuously evaporated in the storage tank, and in order to maintain the pressure of the evaporated gas at an appropriate level, the evaporated gas is discharged through the pipe, and the discharged boil-off gas (NBOG) is a fuel. After being fed and compressed along the supply line L1, it is supplied to the high pressure natural gas injection engines E1 and E2.
- NBOG discharged boil-off gas
- a compressor 100 is configured in the fuel supply line L1 to compress the boil-off gas to be supplied to the engine.
- the compressor 100 may be configured as a multistage compressor in which a compression cylinder and an intermediate cooler are alternately provided.
- 5 shows a multistage compressor 100 in which five compression cylinders and five intermediate coolers are alternately provided.
- the first engine E1 receives fuel for the boil-off gas compressed through a part of the multi-stage compressor 100 and the boil-off gas compressed through the whole of the multi-stage compressor 100 is fueled.
- the second engine E2 supplied with the is provided.
- the first engine E1 is a DF engine capable of supplying the compressed boil-off gas at 5 to 20 bar as fuel, and the second engine E2 can receive the boil-off gas compressed at 150 to 400 bar as the fuel. It may be a ME-GI engine.
- the present embodiments configure the liquefaction line L2 to process the boil-off gas, so that the remaining boil-off gas is supplied as fuel to the first and second engines E2. It is liquefied through the heat exchanger 200 and the expansion means 300 is to be stored in the LNG storage tank (T).
- the heat exchanger 200 is provided at the intersection of the liquefaction line L2 and the fuel supply line L1 to cool the boil-off gas compressed by the compressor 100 by heat exchange with the boil-off gas to be introduced into the compressor 100.
- the high pressure evaporated gas compressed by the compressor 100 is exchanged with the cryogenic evaporated gas immediately after being discharged from the LNG storage tank T to liquefy the high pressure evaporated gas.
- the present embodiments enable the liquefaction of the boil-off gas by cold heat of the boil-off gas itself generated in the LNG storage tank T without a separate refrigerant system.
- the LNG storage tank A gas-liquid separator 400 for supplying T
- the boil-off gas LBOG liquefied by cooling in the heat exchanger 200 is reduced in pressure while passing through the expansion means 300 and is supplied to the gas-liquid separator 400 in a gas-liquid mixed state.
- the expansion means 300 may be, for example, a J-T valve or an expander. While passing through the expansion means 300, LBOG can be reduced to approximately atmospheric pressure.
- the LBOG in the gas-liquid mixed state is separated from the gas and liquid components in the gas-liquid separator 400, so that the liquid component, that is, LNG, is transferred to the LNG storage tank T through the return line L3, and the gas component, that is, evaporation
- the gas is discharged from the storage tank through the recirculation line RL and joins the boil-off gas stream to be supplied to the heat exchanger 200 and the compressor 100.
- Recirculation line RL may be further provided with an expansion valve (V4) for reducing the evaporated gas separated from the gas-liquid separator 400. Separation valve V3 may be provided in return line L3 to open and close the pipe.
- the present embodiment branches the bypass line BL in the liquefaction line L2, so that the adiabatic expansion of the boil-off gas from the downstream of the expansion means 300 can be supplied downstream of the gas-liquid separator 400, Allow for diversification of operations.
- a first separation valve V1 is provided upstream of the gas-liquid separator 400 in the liquefaction line L2, and a second separation valve V2 is provided in the bypass line BL.
- the adiabatic expanded LBOG may be gas-liquid separated through the gas-liquid separator 400 in a two-phase state, and may bypass the bypass line BL without passing through the gas-liquid separator 400.
- the supply line to the return line (L3) is supplied to the LNG storage tank (T) may be further liquefied by the cold heat inside the storage tank.
- the compressor 100 When the amount of boil-off gas generated in the LNG storage tank T is greater than the amount of fuel required by the engine and the amount that can be liquefied, and the excess boil-off gas is expected to occur, the compressor 100 is compressed or compressed in stages.
- the boil-off gas on the way may be supplied to the boil-off gas consumption means G.
- the boil-off gas consumption means G for example, a GCU, a DF Generator, a gas turbine, or the like can be used.
- the cooler 500 is further provided in the recirculation line RL of the third embodiment, so that the boil-off gas cooled in the heat exchanger 200 is separated from the gas-liquid separator 400 prior to adiabatic expansion. Allow for additional cooling with a separate boil-off gas.
- the recirculation line and the liquefaction line (L2) so that the high-pressure liquid evaporated gas passed through the heat exchanger 200 can be further cooled by heat exchange with the low pressure cryogenic gas state separated from the gas-liquid separator 400.
- the first engine E1a that receives the boil-off gas under compression in the compressor is provided, and the boil-off gas compressed through the compressor 100a may be reliquefied. It is a system configured to be. Such a system can increase the amount of boil off gas reliquefaction.
- an engine E1a that consumes a single pressure gas is provided so that the boil-off gas compressed through the compressor 100a is transferred to the engine. It is not supplied but reliquefied. Descriptions overlapping with the above-described embodiment will be omitted.
- the cooler 500a is further provided in the recirculation line RLa of the fifth embodiment, so that the evaporated gas cooled in the heat exchanger 200a is subjected to the gas-liquid separator 400a before the adiabatic expansion.
- the description overlapping with the above-described embodiment is omitted.
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Abstract
Description
Claims (9)
- 선박 또는 부유식 구조물의 LNG 저장탱크에서 발생하는 증발가스를 압축하는 압축기;상기 압축기에서 압축된 상기 증발가스를 상기 압축기로 도입될 증발가스와 열교환으로 냉각시키는 열교환기;상기 열교환기에서 냉각된 상기 증발가스를 단열팽창시키는 팽창수단;상기 팽창수단에서 단열팽창된 상기 증발가스를 기액 분리하고 액화천연가스를 상기 LNG 저장탱크로 공급하는 기액분리기; 및상기 팽창수단의 하류로부터 단열팽창된 상기 증발가스를 상기 기액분리기의 하류로 공급하는 바이패스 라인;을 포함하는, 증발가스 처리 시스템.
- 제 1항에 있어서,상기 기액분리기에서 분리된 기체 상태의 상기 증발가스를 상기 LNG 저장탱크로부터 상기 열교환기로 도입될 상기 증발가스의 흐름으로 도입시키는 재순환 라인; 및상기 재순환 라인에 마련되며 상기 열교환기에서 냉각된 상기 증발가스를 상기 기액분리기에서 분리된 상기 증발가스로 추가 냉각하는 냉각기;를 더 포함하는, 증발가스 처리 시스템.
- 제 1항에 있어서,상기 기액분리기의 상류에 마련되는 제1 분리 밸브; 및상기 바이패스 라인에 마련되는 제2 분리 밸브;를 더 포함하는, 증발가스 처리 시스템.
- 제 1항에 있어서,상기 압축기는 압축실린더와 중간냉각기가 교대로 마련되는 다단 압축기이고,상기 다단 압축기의 일부를 거쳐 압축된 상기 증발가스는 제 1 엔진에 연료로 공급되는 증발가스 처리 시스템.
- 제 4항에 있어서,상기 다단 압축기의 전부를 거쳐 압축된 상기 증발가스는 제2 엔진에 연료로 공급되고,상기 제1 및 제2 엔진에 공급되고 남은 상기 증발가스는 상기 열교환기 및 상기 팽창수단을 거쳐 액화되어 상기 LNG 저장탱크로 저장되는 것을 특징으로 하는, 증발가스 처리 시스템.
- 제 5항에 있어서,상기 제1 엔진은 5 내지 20 bar로 압축된 증발가스를 연료로 공급받을 수 있는 DF 엔진이고, 상기 제2 엔진은 150 내지 400 bar로 압축된 증발가스를 연료로 공급받을 수 있는 ME-GI 엔진인 것을 특징으로 하는, 증발가스 처리 시스템.
- 제 1항에 있어서,상기 팽창수단은 팽창밸브(J-T valve) 및 팽창기(expander) 중 어느 하나인 것을 특징으로 하는, 증발가스 처리 시스템.
- 선박 또는 부유식 구조물의 LNG 저장탱크에서 발생하는 증발가스를 압축하여 선박 또는 부유식 구조물의 엔진으로 공급하는 연료공급 라인;압축된 증발가스의 일부를 분기하여 상기 LNG 저장탱크에서 발생하여 압축될 증발가스와 열교환시켜 냉각하고 단열팽창으로 액화시키는 액화 라인;단열팽창된 상기 증발가스를 기액 분리하고 액화천연가스를 상기 LNG 저장탱크로 공급하는 기액분리기; 및상기 액화 라인으로부터 분기되며 단열팽창된 상기 증발가스를 상기 기액분리기를 우회하여 상기 LNG 저장탱크로 공급하는 바이패스 라인;을 포함하는, 증발가스 처리 시스템.
- 제 8항에 있어서,상기 기액분리기에서 분리된 기체 상태의 상기 증발가스를 상기 연료공급 라인으로 재도입시키는 재순환 라인; 및상기 재순환 라인과 상기 액화 라인의 교차점에 마련되며, 상기 액화 라인에서 압축될 증발가스와 열교환으로 냉각된 상기 증발가스를 상기 기액분리기에서 분리된 상기 증발가스로 추가 냉각하는 냉각기;를 더 포함하는, 증발가스 처리 시스템.
Priority Applications (8)
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CN201580010403.7A CN106029491B (zh) | 2014-02-28 | 2015-02-27 | 蒸发气体处理系统 |
DK15755871.9T DK3112249T3 (da) | 2014-02-28 | 2015-02-27 | System til behandling af boil-off-gas |
US15/110,890 US20160356424A1 (en) | 2014-02-28 | 2015-02-27 | Boil-off gas treatment system |
RU2016138308A RU2642713C1 (ru) | 2014-02-28 | 2015-02-27 | Система обработки отпарного газа |
EP15755871.9A EP3112249B1 (en) | 2014-02-28 | 2015-02-27 | Boil-off gas treatment system |
PCT/KR2015/001916 WO2015130122A1 (ko) | 2014-02-28 | 2015-02-27 | 증발가스 처리 시스템 |
JP2016553893A JP6461988B2 (ja) | 2014-02-28 | 2015-02-27 | 蒸発ガス処理システム |
PH12016501322A PH12016501322A1 (en) | 2014-02-28 | 2016-07-04 | Boil-off gas treatment system |
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KR1020140024460A KR101519541B1 (ko) | 2013-06-26 | 2014-02-28 | 증발가스 처리 시스템 |
KR10-2014-0024460 | 2014-02-28 | ||
PCT/KR2015/001916 WO2015130122A1 (ko) | 2014-02-28 | 2015-02-27 | 증발가스 처리 시스템 |
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US (1) | US20160356424A1 (ko) |
EP (1) | EP3112249B1 (ko) |
JP (1) | JP6461988B2 (ko) |
KR (1) | KR101519541B1 (ko) |
CN (2) | CN107539428A (ko) |
DK (1) | DK3112249T3 (ko) |
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- 2015-02-27 EP EP15755871.9A patent/EP3112249B1/en active Active
- 2015-02-27 RU RU2016138308A patent/RU2642713C1/ru active
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Also Published As
Publication number | Publication date |
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CN106029491A (zh) | 2016-10-12 |
KR101519541B1 (ko) | 2015-05-13 |
KR20150001597A (ko) | 2015-01-06 |
PH12016501322A1 (en) | 2016-08-15 |
CN107539428A (zh) | 2018-01-05 |
EP3112249A1 (en) | 2017-01-04 |
JP6461988B2 (ja) | 2019-01-30 |
EP3112249B1 (en) | 2019-07-03 |
CN106029491B (zh) | 2018-02-06 |
DK3112249T3 (da) | 2019-10-07 |
EP3112249A4 (en) | 2018-04-04 |
US20160356424A1 (en) | 2016-12-08 |
JP2017509845A (ja) | 2017-04-06 |
RU2642713C1 (ru) | 2018-01-25 |
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