WO2018124815A1 - Système d'alimentation en gaz combustible - Google Patents

Système d'alimentation en gaz combustible Download PDF

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Publication number
WO2018124815A1
WO2018124815A1 PCT/KR2017/015736 KR2017015736W WO2018124815A1 WO 2018124815 A1 WO2018124815 A1 WO 2018124815A1 KR 2017015736 W KR2017015736 W KR 2017015736W WO 2018124815 A1 WO2018124815 A1 WO 2018124815A1
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WO
WIPO (PCT)
Prior art keywords
gas
unit
boil
liquefied gas
cooling
Prior art date
Application number
PCT/KR2017/015736
Other languages
English (en)
Korean (ko)
Inventor
송용석
정승재
Original Assignee
삼성중공업 주식회사
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from KR1020170000153A external-priority patent/KR101824421B1/ko
Priority claimed from KR1020170005978A external-priority patent/KR20180083556A/ko
Priority claimed from KR1020170005975A external-priority patent/KR101924535B1/ko
Application filed by 삼성중공업 주식회사 filed Critical 삼성중공업 주식회사
Priority to CN201780082063.8A priority Critical patent/CN110167837B/zh
Priority to SG11201906121RA priority patent/SG11201906121RA/en
Priority to JP2019556779A priority patent/JP6876826B2/ja
Publication of WO2018124815A1 publication Critical patent/WO2018124815A1/fr

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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B25/00—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby
    • B63B25/02—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods
    • B63B25/08—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid
    • B63B25/12—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed
    • B63B25/16—Load-accommodating arrangements, e.g. stowing, trimming; Vessels characterised thereby for bulk goods fluid closed heat-insulated
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63B—SHIPS OR OTHER WATERBORNE VESSELS; EQUIPMENT FOR SHIPPING 
    • B63B35/00—Vessels or similar floating structures specially adapted for specific purposes and not otherwise provided for
    • B63B35/44—Floating buildings, stores, drilling platforms, or workshops, e.g. carrying water-oil separating devices
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B63—SHIPS OR OTHER WATERBORNE VESSELS; RELATED EQUIPMENT
    • B63J—AUXILIARIES ON VESSELS
    • B63J2/00—Arrangements of ventilation, heating, cooling, or air-conditioning
    • B63J2/12—Heating; Cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K15/00—Adaptations of plants for special use
    • F01K15/02—Adaptations of plants for special use for driving vehicles, e.g. locomotives
    • F01K15/04—Adaptations of plants for special use for driving vehicles, e.g. locomotives the vehicles being waterborne vessels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K17/00—Using steam or condensate extracted or exhausted from steam engine plant
    • F01K17/02—Using steam or condensate extracted or exhausted from steam engine plant for heating purposes, e.g. industrial, domestic
    • 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
    • F17C13/00—Details of vessels or of the filling or discharging of vessels
    • 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
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • 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

Definitions

  • the present invention relates to a fuel gas supply system, and more particularly, to a fuel gas supply system for supplying fuel gas using a liquefied gas or an evaporated gas thereof.
  • IMO International Maritime Organization
  • the natural gas is cooled to about -162 degrees Celsius and reduced to a volume of 1/600 by phase change to Liquefied Natural Gas (LNG), a colorless and transparent cryogenic liquid. Is doing.
  • LNG Liquefied Natural Gas
  • the liquefied natural gas is accommodated in a storage tank which is insulated and installed in the hull and stored and transported.
  • a storage tank which is insulated and installed in the hull and stored and transported.
  • the external heat is continuously transferred to the inside of the storage tank so that the evaporated gas generated by the natural vaporization of the liquefied natural gas accumulates inside the storage tank. .
  • the boil-off gas can raise the internal pressure of the storage tank and cause deformation and damage of the storage tank, it is necessary to process and remove the boil-off gas.
  • a method of sending an evaporated gas to a vent mast provided at an upper side of a storage tank, or burning an evaporated gas by using a gas compression unit (GCU) has been used.
  • GCU gas compression unit
  • this is not desirable in terms of energy efficiency. Therefore, the method of supplying the boil-off gas together with the liquefied natural gas or the engine of the ship as fuel gas, or by re-liquefying the boil-off gas using a reliquefaction device composed of a refrigeration cycle, etc. It is used.
  • a floating power generation system includes a recondenser for recondensing evaporated gas generated by liquefied gas from a storage tank in which liquefied gas is stored to be used as a fuel such as a gas turbine for producing electricity of the power generation system.
  • a recondenser for recondensing evaporated gas generated by liquefied gas from a storage tank in which liquefied gas is stored to be used as a fuel such as a gas turbine for producing electricity of the power generation system.
  • floating power generation systems include a vaporizer that vaporizes liquefied gas before supplying it to a gas turbine that generates electricity using liquefied gas.
  • the floating power generation system may include an air cooler for cooling the air supplied to the gas turbine to increase the efficiency of the gas turbine.
  • the thermofluid or cooling fluid used in the carburetor and air cooler and the system for circulating them are generally separate from the cooling system that cools the floating body or other components requiring cooling of the floating power generation system, such as a vessel with a floating power generation system. Is provided.
  • the present invention is to provide a fuel gas supply system capable of effectively recondensing the generated evaporated gas with a small amount of evaporated gas with a large difference depending on the operation mode.
  • the present invention is to provide a fuel gas supply system that can reduce the amount of evaporated gas generated.
  • the present invention is to provide a fuel gas supply system that can utilize a large amount of boil-off gas.
  • the present invention is to provide a fuel gas supply system that can adjust the temperature of the heat source flowing into the vaporizer.
  • the present invention is to provide a fuel gas supply system that can increase the cooling and heating efficiency.
  • the storage unit for receiving the liquefied gas and the boil-off gas generated therefrom;
  • a compression unit which pressurizes and transports the boil-off gas generated in the storage unit;
  • a recondensation unit for recondensing the boil-off gas compressed in the compression unit using the supercooled liquefied gas of the storage unit;
  • a high pressure pump unit installed in a demand source supply line from the recondensation unit to a demand destination to pressurize the liquefied gas of the recondensation unit to a required pressure of the demand destination;
  • a heat exchanger unit having a vaporizer for heating and regasifying the liquefied gas pressurized by the high pressure pump unit, wherein the recondensing unit mixes the liquefied gas transferred from the storage unit and the boiled gas compressed in the compression unit.
  • a first condensation unit for recondensing the boil-off gas And a second condensation unit configured to heat-exchange the liquefied gas pressurized by the high pressure pump unit and the boil-off gas compressed by the compression unit to recondensate the boil-off gas.
  • the compression unit includes a first compression unit for compressing the evaporated gas transported from the storage unit to send to the first condensation unit; And a second compression unit configured to compress the boil-off gas and transfer it to the second condensation unit when the boil-off gas is generated above the recondensation capacity of the first condensation unit.
  • the fuel gas supply system further includes a minimum flow rate line branched from the rear end of the high pressure pump unit and circulated to the first condensation portion, and the second condensation portion branched from the minimum flow rate line and connected to the rear end of the high pressure pump unit again. Installed in the condensation line, it is possible to perform a heat exchange between the liquefied gas passing through the condensation line and the boil-off gas toward the first condensing unit in the compression unit.
  • the boil-off gas recondensed in the second condensation unit may be recovered to the first condensation unit.
  • the first condensation unit may mix the liquefied gas pressurized by the supply pump of the storage unit and the boil-off gas compressed in the first compression unit of the compression unit to condense all or part of the boil-off gas.
  • the compression unit may further include a high-pressure compression unit for compressing a part of the boil-off gas generated in the storage unit to a high pressure to transfer to the demand supply line of the rear end of the vaporizer.
  • the heat exchange unit may further include a heater for heating the fluid passing therethrough at the rear end of the vaporizer to a temperature required by the customer.
  • the liquefied gas supply line for transferring the liquefied gas contained in the storage unit to the first condensing unit;
  • a boil-off gas first supply line for transferring the boil-off gas contained in the storage unit to the first condensation unit through a first compression unit;
  • a second boil-off gas supplying line for transferring the boil-off gas contained in the storage unit to a second condensation unit through a second compression unit;
  • a demand destination supply line for transferring the liquefied gas stored in the first condenser to a demand destination via a high pressure pump unit and a vaporizer;
  • a condensation line branched at a rear end of the high pressure pump unit of the demand source supply line and rejoined to bypass the liquefied gas pressurized by the high pressure pump unit, wherein the second condensation part evaporates the second supply line.
  • a fuel gas supply system may be provided that heat-exchanges a gas and a liquefied gas of the condensation line to recondense the boil-off gas of the second boil-off gas
  • the liquefied gas supply line includes a liquefied gas first supply line and a liquefied gas second supply line, and the first condensing unit injects liquefied gas supplied from the liquefied gas second supply line to the boil-off gas stored therein. Can be recondensed.
  • the fuel gas supply system further includes a minimum flow rate line connected to the first condensing unit at a rear end of the high pressure pump unit of the demand supply line, and the condensation line is branched from the minimum flow rate line to supply the high pressure pump unit of the demand supply line. It may be rejoined later.
  • the fuel gas supply system blocks the flow of fluid from the second supply line, the condensation line, and the demand supply line to the demand destination during operation of the minimum flow rate, wherein the liquefied gas stored in the first condensation unit is blocked.
  • the fuel gas supply system interrupts the flow of fluid to the boil-off gas second supply line and the condensation line during normal operation and stops the operation of the second condensation unit, and the boil-off gas second supply line and By opening the fluid flow to the condensation line and operating the second condensation unit, it may be operated differently depending on the operation mode.
  • the fuel gas supply system may provide an excess amount of boil-off gas when the amount of boil-off gas generated in the storage unit is greater than the amount that can be recondensed by the first condensation unit and the second condensation unit during the loading operation. It may further include a high pressure supply line for supplying the boil-off gas directly by pressurizing the high-pressure compression unit.
  • the fuel gas supply system may further include a heat exchange line provided with a heater for controlling a temperature of the fuel gas supplied to the demand destination, and branched from the supply destination supply line.
  • the fuel gas supply system may further include an evaporation loss module for reducing the evaporation amount of the liquefied gas in the storage unit, wherein the evaporation loss module may include a cooling unit for cooling the storage tank of the storage unit.
  • the cooling unit includes an injection member for injecting liquefied gas stored in the storage tank into the storage tank;
  • An injection pump for supplying the liquefied gas stored in the storage tank to the injection member; It may include an injection line connecting the injection member and the injection pump.
  • the fuel gas supply system further includes a shipping unit for transferring the liquefied gas from the liquefied gas carrier to the storage tank, wherein the evaporation reduction module cools the storage tank before the shipping unit transfers the liquefied gas. It may further comprise a controller for controlling the unit.
  • the controller may control the cooling unit to cool the storage tank while the shipping unit transports liquefied gas.
  • the evaporation loss module may further include a pressure regulating unit for adjusting the pressure in the storage tank.
  • the controller adjusts the pressure to pressurize the inside of the storage tank for a first time before or after the shipping unit starts liquefied gas transfer and maintain the pressure inside the storage tank for a second time after the first time. You can control the unit.
  • the controller may control the pressure regulating unit to depressurize the inside of the storage tank for a third time after the second time.
  • the fuel gas supply system further includes an evaporation gas supply line through which the evaporation gas is transferred from the storage tank to the recondensation unit, wherein the pressure control unit includes a pressure control valve for adjusting the opening rate of the evaporation gas supply line. can do.
  • the demand destination includes a gas power generation module provided with a gas turbine for generating electricity using liquefied gas, and the fuel gas supply system compresses a portion of the boil-off gas in the boil-off gas supply line and supplies the excess gas to the gas turbine. It may further include a supply unit.
  • the fuel gas supply system may further include an boil-off gas conveying unit for conveying a portion of the boil-off gas generated in the storage tank to the liquefied gas carrier.
  • the boil-off gas conveying unit includes: a conveying line provided so that a portion of the boil-off gas generated in the storage tank is conveyed to the liquefied gas carrier; A carrier gas pressurizer for pressurizing the boil-off gas in the carrier line in the direction of the liquefied gas carrier may be included.
  • the boil-off gas conveying unit may further include a bypass line provided so that boil-off gas is transferred to the liquefied gas carrier by bypassing the conveying gas pressurizer from the storage tank.
  • the boil-off gas conveying unit may further include a pressure adjusting member for adjusting the pressure of the liquefied gas storage tank in which the liquefied gas of the liquefied gas carrier is stored.
  • the fuel gas supply system further includes a circulation module for circulating a cooling fluid, the circulation module comprising: a main circulation module for circulating the cooling fluid to cool a cooling object; It may include an auxiliary circulation module for circulating the cooling fluid to be introduced into the vaporizer by branching the cooling fluid circulated by the main circulation module to heat exchange with the liquefied gas in the vaporizer.
  • the consumer includes a gas power generation module provided with a gas turbine for generating electricity by using liquefied gas, the gas power generation module including an air cooler for cooling external air flowing into the gas turbine, wherein the auxiliary circulation module
  • the cooling fluid after the heat exchange with the liquefied gas in the vaporizer may be introduced into the air cooler to circulate the cooling fluid to exchange heat with the outside air.
  • the main circulation module includes a cooling unit for cooling the cooling fluid; A main circulation pipe through which the cooling fluid is circulated between the cooling unit and the cooling target; It may include a main pump for applying pressure to the cooling fluid to flow the cooling fluid along the main circulation pipe.
  • the auxiliary circulation module includes a temperature regulating unit for controlling a temperature of the cooling fluid flowing into the vaporizer, wherein the temperature regulating unit includes the first fluid and the cooling fluid which is the cooling fluid flowing from the cooling unit to the cooling target.
  • a mixing member to which a second fluid which is the cooling fluid flowing from the object to the cooling unit is mixed;
  • a controller for controlling the mixing member to adjust the mixing ratio between the first fluid and the second fluid according to the temperature of the outside air and the temperature of the cooling fluid introduced into the vaporizer.
  • a third fluid which is a cooling fluid in which heat exchange is completed with the liquefied gas in the vaporizer, is mixed with the first fluid and the second fluid, and the controller is configured to control the temperature of the outside air and the cooling fluid introduced into the vaporizer. According to the temperature, the mixing member may be controlled to adjust the mixing ratio between the first fluid, the second fluid and the third fluid.
  • the auxiliary circulation module may comprise a bypass flow passage provided for the cooling fluid to bypass the air cooler.
  • the auxiliary circulation module may circulate the cooling fluid such that the cooling fluid passing through the air cooler or the bypass passage is mixed with the first fluid and supplied to the cooling target.
  • the controller may adjust the flow rate of the cooling fluid flowing into the vaporizer in accordance with the temperature of the outside air and the temperature of the cooling fluid flowing into the vaporizer.
  • the fuel gas supply system further includes a circulation module for circulating the cooling fluid and the intermediate fruit, the circulation module comprising: a main circulation module for circulating the cooling fluid to cool a cooling object; An auxiliary circulation module for circulating the intermediate fruit to vaporize the liquefied gas in the vaporizer; It may include a heater for heating the intermediate fruit by heat exchange between the cooling fluid circulated by the main circulation module and the intermediate fruit circulated by the auxiliary circulation module.
  • the consumer includes a gas power generation module provided with a gas turbine for generating electricity by using liquefied gas, the gas power generation module including an air cooler for cooling external air flowing into the gas turbine, wherein the auxiliary circulation module
  • the intermediate fruit after the heat exchange with the liquefied gas in the vaporizer may be introduced into the air cooler to circulate the intermediate fruit to exchange heat with the outside air.
  • the auxiliary circulation module includes a temperature control unit for controlling the temperature of the intermediate fruit flowing into the vaporizer, wherein the temperature control unit includes: a bypass tube provided to flow the intermediate fruit bypassing the heater; A control valve for controlling the flow of the intermediate fruit to the bypass pipe; According to the temperature of the outside air and the temperature of the intermediate fruit is heated by the heater and introduced into the vaporizer, it may include a controller for controlling the flow of the intermediate fruit by controlling the control valve.
  • Fuel gas supply system can be supplied to the demand (HP Fuel Gas Consumer) by regasifying the liquefied gas, reducing the emissions of sulfur oxides (SOx), nitrogen oxides (NOx), etc. to reduce the cost of the exhaust gas treatment equipment can do.
  • HP Fuel Gas Consumer HP Fuel Gas Consumer
  • SOx sulfur oxides
  • NOx nitrogen oxides
  • the boil-off gas generated during operation can be recovered and used as fuel.
  • the second compression unit (Aux. LP BOG Compressor) and the second condensation unit (Aux. BOG Recondenser) can be recondensed and recovered.
  • the liquefied gas passing through the second condensation unit is pressurized by a high pressure pump unit (HP LNG Booster Pump) and sufficiently cooled, the boil-off gas (BOG) transferred from the second compression unit to the first condensation unit during the loading operation. Evaporative gas is not generated even when heat exchanged with, which enables efficient fuel gas supply.
  • HP LNG Booster Pump high pressure pump unit
  • BOG boil-off gas
  • a part of the liquefied gas passing through the high-pressure pump unit condenses the evaporated gas in the second condensation unit, so that the evaporated gas is recondensed without an additional energy source, so that no separate reliquefaction apparatus is required. This also minimizes the energy required for reliquefaction.
  • a second condensation unit (Aux. BOG Recondenser) is installed to recondensate the excess evaporated gas generated during the loading operation, but is installed in a condensation line branched from the minimum flow line. Quantity can be minimized.
  • the compression unit may be classified according to the operating state by providing a first compression unit (first low compression unit), a second compression unit (second low compression unit), and three high compression units.
  • first low compression unit first low compression unit
  • second low compression unit second low compression unit
  • three high compression units when the excess evaporation gas is generated unlike in the normal operation such as during the loading operation, the second low compression unit is used for the remaining evaporation gas more than the capacity of the first compression unit to handle the first low compression.
  • the part and the second low compression part are in charge.
  • the high-pressure compression unit may be applied and used for the remaining boil-off gas.
  • energy consumption may be reduced by transferring the recondensed evaporated gas through the second condenser (Aux. BOG Recondenser) to the first condenser (Main BOG Recondenser) instead of the storage tank.
  • the recondensed boil-off gas is returned to the low pressure storage tank, it is necessary to pressurize the feed pump again in the low pressure (5 kPag) environment and transfer it to the first condensation unit, thereby reducing energy waste.
  • FIG. 1 shows a fuel gas supply system according to a first embodiment of the present invention.
  • FIG. 2 shows a fuel gas supply system according to a second embodiment of the present invention.
  • FIG 3 shows a normal operating state of a fuel gas supply system according to a second embodiment of the present invention.
  • FIG. 4 shows a minimum flow rate operating state of a fuel gas supply system according to a second embodiment of the present invention.
  • FIG 5 shows a loading operation state of a fuel gas supply system according to a second embodiment of the present invention.
  • FIG. 6 shows a fuel gas supply system according to a third embodiment of the present invention.
  • FIG. 7 shows a fuel gas supply system according to a fourth embodiment of the present invention.
  • FIG 8 shows a fuel gas supply system according to a fifth embodiment of the present invention.
  • FIG 9 shows a fuel gas supply system according to a sixth embodiment of the present invention.
  • FIG. 10 is a block diagram illustrating the temperature control unit of FIG. 9.
  • FIG 11 shows a fuel gas supply system according to a seventh embodiment of the present invention.
  • FIG. 12 shows a fuel gas supply system according to an eighth embodiment of the present invention.
  • FIG. 13 is a block diagram illustrating the temperature control unit of FIG. 12.
  • FIG. 14 shows a fuel gas supply system according to a ninth embodiment of the present invention.
  • the storage unit 100 for receiving the liquefied gas and the evaporated gas generated therefrom, the compression unit 200 for pressurizing and transporting the boiled gas generated in the storage unit 100, the compression unit (Recondensing unit 300 for recondensing the boil-off gas compressed in the 200 using the supercooled liquefied gas of the storage unit 100, from the recondensation unit 300 to the customer destination supply line (L30) leading to the customer destination (10)
  • a high-pressure pump unit 400 installed to pressurize the liquefied gas of the recondensing unit 300 to the required pressure or more of the demand destination 10, and a vaporizer 510 for heating and re-vaporizing the liquefied gas pressurized by the high-pressure pump unit 400.
  • the recondensation unit 300 is to condensate the evaporation gas by mixing the liquefied gas transported from the storage unit 100 and the boiled gas compressed in the compression unit 200 Pressurized by the first condenser 310 and the high pressure pump unit 400
  • the second may comprise a condensing unit 320 to control the heat exchange the compressed boil-off gas in a liquefied gas transport and the compression unit 200, which is to re-condense the boil-off gas.
  • the fuel gas supply system for transferring the liquefied gas contained in the storage unit 100 to the first condensation unit 310, the storage unit 100 )
  • the first boil-off gas (L21) to transfer the boil-off gas contained in the first compression unit (210) to the first condensation unit (310), the second boil-off unit (evaporated gas received in the storage unit 100).
  • the demand destination 10 is a gaseous state of the liquefied gas accommodated in the storage unit 100 through the boil-off gas supply line (L20) or liquefied gas supply line (L10) to be described later, evaporated gas or natural evaporated gas, etc.
  • It may be an engine that receives fuel gas and generates propulsion of a ship.
  • the engine may be a gas turbine that is a rotary heat engine that is operated by combustion gas of high temperature and high pressure, a high pressure gas injection engine such as a ME-GI engine, or a fuel gas having a medium pressure of about 15 to 17 bar, specifically, a fuel gas.
  • An X-DF engine capable of generating an output may be used, but the present invention is not limited thereto, and includes an engine having various types of engines if the fuel gas is generated in a gaseous state.
  • the gas compression unit (GCU) 20 may consume fuel gas by receiving a fluid pressurized by the first compression unit 210 from the boil-off gas first supply line L21 and incinerating it.
  • the storage unit 100 may include a plurality of storage tanks 101 arranged in parallel. At this time, each storage tank 101 receives the liquefied fuel from the production site of the natural gas and the like, and stores and stores the liquefied fuel stably until the destination is unloaded.
  • the storage tank 101 may be provided with a cargo hold of the membrane type heat-insulated treatment so as to minimize the vaporization of the liquefied fuel by the external heat intrusion.
  • the liquefied fuel stored in the storage tank 101 may be used as fuel gas, such as a ship's propulsion engine, a power generation engine, and a GCU, as described below.
  • the supply pump 110 may be provided at an inlet end of the liquefied gas supply line L10 in the storage tank 101, but may be provided adjacent to a bottom surface of the storage tank 101 to improve operating efficiency.
  • the supply pump 110 may send the liquefied gas contained in the storage tank 101 to the liquefied gas supply line L10.
  • the circulation line 120 returns a portion of the liquefied gas supplied to the liquefied gas supply line L10 through the supply pump 110 back to the storage tank 101, so that the amount or amount of liquefied gas in the first condensation unit 310 is
  • the amount of liquefied gas supplied to the first condenser 310 may be adjusted according to the amount of fuel required by 10.
  • the compression unit 200 compresses the boil-off gas transferred from the storage unit 100 and sends the first-compression unit 210 to the first condensation unit 310, and the re-condensation of the boil-off gas to the first condensation unit 310. It may include a second compression unit 220 for transferring the boil-off gas to the second condensation unit 320 when the capacity exceeds the capacity.
  • the first compression unit 210 may be provided on the boil-off gas first supply line L21, and the second compression unit 220 may be provided on the boil-off gas second supply line L22.
  • the first compression unit 210 is always operated according to the operation mode of the fuel gas supply system, and the second compression unit 220 may be operated only during the loading operation. Since a large amount of boil-off gas is generated in the storage unit 100 during the loading operation, the second compression unit 220 and the first compression unit 210 are operated together.
  • the recondensation unit 300 will be described.
  • the recondensation unit 300 largely includes a first condensation unit 310 and a second condensation unit 320.
  • the first condenser 310 may serve as a reservoir for temporarily storing the liquefied gas supplied from the liquefied gas supply line L10. Furthermore, the first condensation unit 310 mixes the liquefied gas pressurized by the supply pump 110 of the storage unit 100 and the boil-off gas compressed by the first compression unit 210 of the compression unit 200, All or part of the boil-off gas may be recondensed. In this case, the recondensation of the introduced boil-off gas may be implemented by injection of the liquefied gas supplied through the liquefied gas second supply line (L12).
  • the second condensing unit 320 is provided in the condensation line L41 to be described later, and the high pressure pump unit in the demand source supply line L30 through heat exchange with the boil-off gas first supply line L21 and the second supply line L22.
  • the liquefied gas pressurized by 400 may be used to recondense the boil-off gas that passes through the boil-off gas second supply line L22 to the first condensation unit 310.
  • the high pressure pump unit 400 sends the liquefied gas contained in the first condenser 310 to the demand source supply line L30 and liquefies the pressure level corresponding to the pressure condition of the fuel gas required by the demand source 10.
  • the gas can be pressurized.
  • the high pressure pump unit 400 may pressurize the liquefied gas to about 30 to 40 barg and send it toward the vaporizer 510.
  • the heat exchange unit 500 includes a vaporizer 510 to vaporize the liquefied gas supplied from the first compression unit 210 toward the demand destination 10 through the supply destination L30.
  • the heat exchange unit 500 may further include not only the vaporizer 510 but also a heater 520 that heats the fluid passing through the vaporizer 510 at the rear end of the vaporizer 510 to a temperature required by the customer 10.
  • the heat exchange line (L31) is further provided in the demand source supply line (L30), the heater 520 is provided on the heat exchange line (L31), the fuel supplied to the demand source 10 through the demand source supply line (L30).
  • the temperature of the gas can be controlled.
  • the heat exchange line L31 may constantly supply the fuel supplied to the demand destination 10 through the demand destination supply line L30 at a temperature required by the demand destination 10.
  • the liquefied gas supply line L10 connects the storage unit 100 and the recondensation unit 300 described above. Specifically, the liquefied gas supply line (L10) supplies the fuel gas sent from the supply pump 110 provided at one end to the first condensation unit (310).
  • the liquefied gas supply line L10 may include a liquefied gas first supply line L11 and a liquefied gas second supply line L12.
  • the liquefied gas first supply line (L11) is branched from the liquefied gas supply line (L10) is connected to the lower portion of the first condensation unit 310, the liquefied gas second supply line (L12) is a liquefied gas supply line (L10) Branched from and connected to the upper portion of the first condensation part 310, the liquefied gas is injected onto the first condensation part 310 to recondensate the boil-off gas supplied into the first condensation part 310.
  • the boil-off gas supply line L20 supplies the boil-off gas stored in the storage unit 100 to the compression unit 200, but branches to the boil-off gas first supply line L21 and the boil-off gas second supply line L22 at a later stage. Can be.
  • the boil-off gas first supply line L21 may extend toward the GCU 20 in the boil-off gas supply line L20.
  • a first compression unit 210 may be provided in the boil-off gas first supply line L21 to pressurize and supply the boil-off gas toward the GCU 20.
  • the boil-off gas first supply line L21 extends toward the GCU 20 and may transfer a portion of the boil-off gas to the first branch line L21a and the second branch line L21b.
  • the first branch line L21a connects the boil-off gas first supply line L21 and the boil-off gas second supply line L22
  • the second branch line L21b connects the boil-off gas first supply line L21.
  • the first condensing unit 310 may be connected to each other to transfer the boil-off gas to the second boil-off gas supply line L22 or the first condensing unit 310.
  • the boil-off gas second supply line L22 may extend from the boil-off gas supply line L20 to the first condensation part 310 via the second compression part 220 and the second condensation part 320.
  • the second boil-off gas supply line L22 is used only when an excessive amount of boil-off gas is generated in the storage tank 101 to be treated in the boil-off gas first supply line L21, and thus the first boil-off gas first supply line L21. The amount of fluid passing through it can be relatively small compared to).
  • the boil-off gas passing through the boil-off gas second supply line L22 may be re-condensed in the second condensation unit 320 and recovered to the first condensation unit 310.
  • the demand source supply line L30 pressurizes the liquefied gas that has passed through the first condensation part 310 through the high pressure pump unit 400, and vaporizes the pressurized liquefied gas with the vaporizer 510 to supply it to the demand destination 10.
  • a minimum flow rate line L40 connected to the first condenser 310 is provided, and the condensation line L41 branches from the minimum flow rate line L40. And it can be rejoined to the rear end of the high-pressure pump unit 400 of the supply line (L30).
  • the minimum flow rate line L40 may be a line for returning the liquefied gas back to the first condenser 310 at the rear end of the high pressure pump unit 400 of the supply source L30. There is a minimum flow rate that the high pressure pump unit 400 can continuously transfer without problems, such as failure, by securing a minimum flow rate line (L40) for flowing this high pressure pump unit 400 before the normal operation state or standby state It is to be able to drive without difficulty.
  • Condensation line (L41) is a second condensing unit 320 is installed to recondensate the excess boil off gas generated in the loading operation (Loading Operation) mode to be described later, the minimum flow line (L40, Minimum Flow) It can be installed branched off the line.
  • FIG. 2 shows a fuel gas supply system according to a second embodiment of the present invention. Description of the second embodiment will be described below to be the same as the description of the fuel gas supply system according to the first embodiment except for the additional description with a separate reference numeral will be described in order to avoid duplication of content. Omit.
  • boil-off gas when the boil-off gas is excessively generated in the storage tank 101 in the boil-off gas supply line (L20), it is pressurized by the high-pressure compressor 230 to the rear end of the vaporizer 510 of the demand source supply line (L30)
  • a high pressure supply line (L23) for supplying boil-off gas may be provided. This functions as a means for supplying the boil-off gas directly to the demand destination 10 when the boil-off gas is excessively generated in a loading operation mode to be described later.
  • FIG. 3 shows a normal operation state of a fuel gas supply system according to a second embodiment of the present invention
  • FIG. 4 shows a minimum flow rate operating state of a fuel gas supply system according to a second embodiment of the present invention
  • FIG. A loading operation state of the fuel gas supply system according to the second embodiment of the present invention is shown.
  • the fuel gas supply system according to the second embodiment of the present invention may be operated in three operation modes, namely, a normal operation mode, a minimum flow rate operation mode, and a shipment operation mode.
  • the liquefied gas stored in the first condenser 310 is blocked by the flow of the boil-off gas from the second supply line L22, the condensation line L41, and the supply source L30 to the demand source 10. Gas is circulated through the high pressure pump unit 400 through the minimum flow line (L40), it is possible to enable the continuous operation of the high pressure pump unit 400.
  • the fluid flow to the second boil-off gas supply line (L22) and the condensation line (L41) is blocked and the second condensing unit (320) is stopped.
  • the second condensing unit (320) By opening the fluid flow to the L22) and the condensation line (L41) and operating the second condensation unit 320, it can be operated differently depending on the operation mode.
  • the operation of each of these modes will be described in detail.
  • the liquefied gas is pressurized by the supply pump 110 to a predetermined pressure and transferred to the first condensation unit 310. At this time, since the liquefied gas is pressurized, it is in a state of supercooling at the corresponding pressure, and the liquid state can be maintained even if the temperature rises to some extent.
  • Boil-off gas is generated in the storage tank 101 for storing the liquefied gas, the thickness of the insulation (insulation) provided in the storage tank 101, the size of the storage tank 101, outside conditions, liquefaction
  • the amount of generated evaporated gas varies depending on the gas storage capacity.
  • the maximum amount of boil-off gas (NBOG) is a conservative condition according to the storage capacity of the liquefied gas according to the storage state because the insulation thickness and the size and outside conditions of the storage tank 101 are fixed at design time. Can be calculated from
  • the boil-off gas is pressurized by the first compression unit 210 in the boil-off gas first supply line L21 and transferred to the first condensation unit 310.
  • the boil-off gas is recondensed by the supercooled liquefied gas transferred from the storage tank 101 through the supply pump 110 in the first condenser 310.
  • the liquefied gas and the recondensed boil-off gas in the first condensation part 310 are sufficiently pressurized by the high pressure pump unit 400 to satisfy the required pressure of the demand destination 10.
  • the liquefied gas pressurized to high pressure is regasified in the vapor phase in the vaporizer 510.
  • the heat source may be sea water, heated cooling water and the like.
  • the temperature of the fuel gas regasified by the heater 520 is heated to a temperature required by the customer 10.
  • the heat source at this time may be steam or the like.
  • the high pressure pump unit 400 may be operated without turning off, which means that a part of the liquefied gas stored in the first condensation unit 310 is transferred to the high pressure pump unit 400 and the minimum flow line L40.
  • the first condensation unit 310 may serve to temporarily store the liquefied gas and separate the evaporated gas, such as a suction drum, instead of recondensing.
  • the liquefied gas is not large enough to recondense the evaporated gas and the recirculation through the minimum flow line (L40) is repeated, and thus the condensed gas cannot be recondensed. If incinerated or impossible, it may be vented.
  • the first condenser 310 Only the evaporation gas that can control the pressure and level of the first condenser 310 is sent to the first condenser 310 by using the first LP compressor (Main LP evaporator gas compressor).
  • the first low compression unit (Main LP boil-off gas compressor) and the second low compression unit (Aux. LP boil-off gas compressor) are transferred to the second condenser 320 to condense the entire amount.
  • the cold source is the liquefied gas pressurized by the high pressure pump unit 400 and branched from the minimum flow line L40 to be supplied to the second condenser 320.
  • the amount of boil-off gas that can be recondensed in the second condenser 320 is first transferred to the second condenser 320, and the remaining amount of the evaporated gas is transferred to the first condenser 310 to condense.
  • the operation is performed as in the case of 2), but the amount of recondensation in the two condensation units 310 and 320 is directly connected to the rear end of the vaporizer 510 by directly pressurizing the high pressure using the high pressure compressor 230. It can be transferred to the demand destination (10).
  • the operation of the fuel gas supply system according to the present invention has been described above.
  • the liquefied gas can be regasified and supplied to the demand destination (10, HP Fuel Gas Consumer)
  • the emission of sulfur oxides (SOx), nitrogen oxides (NOx), and the like can be reduced, thereby reducing the cost of the exhaust gas treatment equipment. .
  • the boil-off gas generated during operation can be recovered and used as fuel.
  • the evaporation gas generated in various operations, in particular, excessively generated during the loading operation may be recondensed and recovered using the second compression unit 220 and the second condensation unit 320. Can be.
  • the boil-off gas generated in various operations may be recondensed and recovered by using the second compression unit 220 and the second condensation unit 320. have. If the fuel is directly pressurized to high pressure without recondensation, the energy consumption required for compression increases, which is a big advantage in terms of energy efficiency. It is thermodynamically clear that evaporation of the liquid after pressurization requires less energy than pressurizing the gas.
  • the first condensation unit 310 is discharged from the second compression unit 220. It is possible to supply fuel gas efficiently without generating boil-off gas even if it exchanges heat with boil-off gas (BOG).
  • the high pressure pump unit 400 HP LNG Booster Pump
  • the second condensing unit 320 is installed to recondensate the excess boil off gas generated during the loading operation, but is installed in the condensation line (L41) branched from the minimum flow line (L40). To minimize the amount of piping.
  • the amount of the second condensation unit 320 can be reduced and the size can be minimized.
  • the second compression unit may be configured for the remaining evaporation gas having a capacity that the first compression unit 210 (the first low compression unit) can handle.
  • the first compression unit 210 and the second compression unit 220 are responsible for transporting the boil-off gas.
  • the high-pressure compressor 230 may be applied and used for the remaining boil-off gas.
  • energy consumption may be reduced by transferring the recondensed evaporated gas to the first condenser 310 instead of the storage tank.
  • the recondensed boil-off gas is returned to the low pressure storage tank 101, it is necessary to pressurize it back to the supply pump 110 in the low pressure (5 kPag) environment and transfer it to the first condensation part. It can be reduced.
  • FIG. 6 shows a fuel gas supply system according to a third embodiment of the present invention.
  • a description will be given of a fuel gas supply system according to an embodiment of the present invention taking the case applied to the floating power generation system as an example.
  • the fuel gas supply system according to the embodiment of FIG. 6 differs from the above-described embodiments in that the fuel gas supply system further includes a shipping unit 50, an evaporation reduction module 5000, and an evaporation gas conveying unit 6000. have.
  • the floating power generation system is installed in a floating body to generate electricity using liquefied gas.
  • Floating bodies may be provided in ships or offshore structures in which they are suspended in water or river water, and the floating power generation system is installed.
  • the floating power generation system includes a storage tank 30, a gas power generation module 2000, a gas supply module 3000, a shipping unit 50, an evaporation loss module 5000, and an evaporation gas conveying unit 6000. ).
  • the floating power generation system includes essential components such as a pump, a compressor, and a valve, which are naturally required for the operation of the floating power generation system.
  • Liquefied gas is stored in the storage tank 30.
  • Storage tank 30 corresponds to a storage unit for receiving liquefied gas and its boil-off gas.
  • Liquefied gas is a flammable substance in which gaseous gas is condensed in a liquid state at room temperature.
  • liquefied gas is provided as liquefied natural gas (LNG).
  • the gas power generation module 2000 corresponds to a demand source of fuel gas.
  • the gas power generation module 2000 generates electricity using the liquefied gas supplied from the storage tank 30.
  • the gas power generation module 2000 has a gas turbine 2100.
  • the gas turbine 2100 produces electricity by burning a liquefied gas supplied in a gaseous state from the storage tank 30 to rotate a turbine.
  • rotation of a turbine of a predetermined rpm or more is generally required.
  • the gas power generation module 2000 is provided with a starter (not shown) for rotating the turbine of the gas turbine 2100 above the predetermined ALPM before the gas turbine 2100 combusts the liquefied gas and operates itself.
  • the gas power generation module 2000 may include an engine instead of the gas turbine 2100.
  • the engine generates electricity by using liquefied gas vaporized in the same manner as the gas turbine 2100, but is different from the gas turbine 2100 in operating conditions.
  • the gas supply module 3000 supplies the liquefied gas stored in the storage tank 30 to the engine.
  • the gas power generation module 2000 may further include an air cooler (not shown).
  • the air cooler cools external air introduced to the gas turbine 2100 for combustion of the liquefied gas. As the temperature of the air flowing into the gas turbine 2100 is lowered, the mass of the air supplied to the gas turbine for the same time increases to increase the output of the gas turbine.
  • the air cooler may not be selectively provided.
  • the gas supply module 3000 supplies the liquefied gas stored in the storage tank 30 to the gas turbine 2100.
  • the gas supply module 3000 includes a recondensation unit 3100, a demand source supply line 3200, a vaporizer 3300, a supply pump 3400, a liquefied gas supply line 3500, and an evaporative gas supply line. 3600.
  • the recondensation unit 3100 recondenses the boil-off gas generated from the liquefied gas in the storage tank 30. Inside the recondensation unit 3100, an evaporated gas in which the liquefied gas is evaporated from the storage tank 30 is supplied from an upper portion, and a liquefied gas in a liquid state is supplied from the storage tank 30.
  • the boil-off gas supplied to the recondensation unit 3100 is cooled through heat exchange with the liquefied gas in the liquid state at high pressure and condensed in the liquid state. According to one embodiment, some of the liquid liquefied gas supplied into the recondensation unit 3100 is sprayed and supplied in the recondensation unit 3100. Therefore, the contact area with the boil-off gas is increased, so that heat exchange between the liquid liquefied gas and the boil-off gas is easier.
  • the customer supply line 3200 connects the recondensation unit 3100 and the gas turbine 2100. Therefore, the liquefied gas condensed in the recondensation unit 3100 is vaporized in the vaporizer 3300 through the supply source line 3200 is supplied to the gas turbine 2100.
  • the high pressure pump unit 3210 may be installed in the supply source 3200. The high pressure pump unit 3210 applies pressure to the liquefied gas so that the liquefied gas in the recondensation unit 3100 is transferred to the gas turbine 2100.
  • the vaporizer 3300 vaporizes the liquefied gas before it is supplied to the gas turbine 2100 so that it can be used as fuel in the gas turbine 2100.
  • the vaporizer 3300 is installed in the supply line 3200 of the customer.
  • the supply pump 3400 transfers the liquefied gas in the storage tank 30 to the recondensation unit 3100. That is, the supply pump 3400 applies pressure to the liquefied gas so that the liquefied gas in the liquid state in the storage tank 30 is moved to the recondensing unit 3100 along the liquefied gas supply line 3500.
  • the liquefied gas supply line 3500 connects the supply pump 3400 and the recondensation unit 3100. Therefore, the liquefied gas pressurized by the supply pump 3400 is transferred to the recondensing unit 3100 along the liquefied gas supply line 3500.
  • the boil-off gas supply line 3600 connects the storage tank 30 and the recondensation unit 3100.
  • the boil-off gas generated in the storage tank 30 is transferred to the recondensation unit 3100 along the boil-off gas supply line 3600 by the pressure in the storage tank 30.
  • the boil-off gas supply line 3600 may be provided with a compression unit 3700.
  • the compression unit 3700 compresses the boil-off gas transferred from the storage tank 30 to the re-condensation unit 3100 before the boil-off gas generated in the storage tank 30 is supplied to the re-condensation unit 3100.
  • the boil-off gas can be more easily condensed in the recondensation unit 3100, and it is easy to maintain the pressure inside the re-condensation unit 3100.
  • the gas supply module 3000 may further include a gas temperature controller (not shown).
  • the gas temperature controller heats the liquefied gas vaporized in the vaporizer 3300 to a temperature at which the efficiency of the gas turbine 2100 is optimized and supplies the gas turbine 2100 to the gas turbine 2100.
  • the shipping unit 50 transfers the liquefied gas from the liquefied gas carrier 40 to the storage tank 30.
  • the liquefied gas carrier 40 is a vessel for transporting liquefied gas to the floating power generation system.
  • the shipping unit 50 includes a transfer line through which liquefied gas is transferred from the liquefied gas carrier 40 to the storage tank 30.
  • the shipping unit 50 may further include a valve (not shown) that opens and closes the transfer line, and a sensor (not shown) which transmits a signal to the controller 5300 whether the shipment is in progress.
  • the evaporation loss module 5000 reduces the amount of evaporated liquefied gas in the storage tank 30.
  • the evaporation loss module 5000 may reduce the evaporation amount of the liquefied gas in the storage tank 30 by cooling the storage tank 30 and pressurizing the internal pressure of the storage tank 30.
  • the evaporation loss module 5000 includes a cooling unit 5100, a pressure regulation unit 5200 and a controller 5300.
  • the cooling unit 5100 cools the storage tank 30.
  • the storage tank 30 may have a larger amount of liquefied gas than the minimum amount that can be transferred to the supply pump 3400.
  • the cooling unit 5100 may cool the storage tank 30 by spraying the liquefied gas in a liquid state stored in the storage tank 30 into the storage tank 30.
  • the cooling unit 5100 includes an injection member 5110, an injection pump 5120, an injection line 5130 and a temperature meter 5140.
  • the injection member 5110 injects the liquefied gas in the liquid state stored in the storage tank 30 into the storage tank 30.
  • the injection pump 5120 applies pressure to the liquefied gas in the storage tank 30 so that the liquefied gas stored in the storage tank 30 is supplied to the injection member 5110.
  • the injection line 5130 connects the injection member 5110 and the injection pump 5120. Therefore, the liquefied gas pressurized by the injection pump 5120 is transferred to the injection member 5110 through the injection line 5130.
  • the temperature measuring device 5140 measures the temperature inside the storage tank 30.
  • the temperature measuring unit 5140 transmits the measured value measuring the temperature of the storage tank 30 to the controller 5300 in real time.
  • the pressure regulating unit 5200 adjusts the pressure in the storage tank 30.
  • the pressure regulating unit 5200 may adjust the pressure in the storage tank 30 by adjusting the flow rate of the boil-off gas transferred from the storage tank 30 to the recondensation unit 3100.
  • the pressure regulating unit 5200 includes a pressure regulating valve 5210 and a pressure meter 5220.
  • the pressure regulating valve 5210 adjusts the opening rate of the boil-off gas supply line 3600. For example, when the opening ratio of the pressure regulating valve 5210 is lowered, since the amount of generated evaporated gas discharged to the outside of the storage tank 30 is reduced, the internal pressure of the storage tank 30 may increase. In addition, when the opening ratio of the pressure regulating valve 5210 is increased, the amount of the generated evaporated gas discharged to the outside of the storage tank 30 increases, so that the internal pressure of the storage tank 30 may decrease.
  • the pressure gauge 5220 measures the pressure inside the storage tank 30.
  • the pressure measuring unit 5220 transmits the measured value measuring the pressure of the storage tank 30 to the controller 5300 in real time.
  • the controller 5300 controls the cooling unit 5100 and the pressure regulating unit 5200.
  • the controller 5300 controls the cooling unit 5100 to cool the inside of the storage tank 30.
  • the controller 5300 controls the cooling unit 5100 to cool the storage tank 30 before the shipping unit 50 starts transferring the liquefied gas from the liquefied gas carrier 40 to the storage tank 30.
  • the controller 5300 operates the injection pump 5120 and opens the injection line 5130 to inject the liquefied gas through the injection member 5110 in the storage tank 30.
  • the controller 5300 controls the cooling unit 5100 to inject liquefied gas for a sufficient time so that the temperature of the storage tank 30 is cooled to a preset temperature.
  • the controller controls the cooling unit 5100 to inject liquefied gas until the storage tank 30 is cooled to -160 ° C.
  • the controller 5300 may control the cooling unit 5100 to cool the storage tank 30 while the shipping unit 50 transfers the liquefied gas from the liquefied gas carrier 40 to the storage tank 30.
  • Can be By continually cooling the storage tank not only before the shipping unit 50 starts to transfer to the storage tank 30 but also during the transfer, the liquefaction of the storage tank 30 while the shipping unit 50 transfers the liquefied gas. It prevents the temperature of the area which is not in contact with the gas from rising.
  • the controller 5300 controls the cooling unit 5100 when cooling the storage tank 30 is described before the storage tank 30 starts to transfer the liquefied gas. It is the same as when cooling.
  • the controller 5300 controls the pressure regulating unit 5200 to adjust the pressure in the storage tank 30. For example, the controller pressurizes the inside of the storage tank 30 for the first time before or after the shipping unit 50 starts to transfer the liquefied gas, and the storage tank 30 for the second time after the first time.
  • the pressure regulating unit 5200 is controlled to maintain the pressure inside.
  • the controller 5300 may control the pressure regulating unit 5200 to depressurize the inside of the storage tank for a third time after the second time.
  • the first time may be a time before or after the shipping unit 50 starts liquefied gas transfer, until the pressure in the storage tank 30 reaches the set pressure.
  • the set pressure may be at least 15 kPaG.
  • the second time may be a time until the time when the shipping unit 50 finishes transferring the liquefied gas after the first time.
  • the controller 5300 adjusts the pressure to reduce the pressure in the storage tank 30 to a suitable pressure for supplying liquefied gas to the configuration required for power generation such as the recondensation unit 3100 and the gas turbine 2100 for the third time.
  • the unit 5200 may be controlled.
  • the controller 5300 controls the opening rate of the pressure regulating valve 5210 so that the boil-off gas generated in the storage tank 30 is recondensed through the boil-off gas supply line 3600. By adjusting the amount to be transferred to), the pressure in the storage tank 30 is adjusted.
  • the controller 5300 lowers the opening rate of the pressure regulating valve 5210, the amount of the boil-off gas in the storage tank 30 is transferred to the recondensation unit 3100 is reduced, thereby reducing the pressure of the storage tank 30. Can be high.
  • the controller 5300 increases the opening rate of the pressure regulating valve 5210, the amount of the boil-off gas in the storage tank 30 is transferred to the recondensation unit 3100 increases so that the pressure of the storage tank 30 is increased. Can be lowered.
  • the storage tank 30 is cooled and pressurized by the evaporation reduction module 5000, thereby reducing the amount of evaporated gas generated in the storage tank 30.
  • the boil-off gas conveying unit 6000 conveys a portion of the boil-off gas generated in the storage tank 30 to the liquefied gas carrier 40. A portion of the boil-off gas generated in the storage tank 30 by the boil-off gas conveying unit 6000 is conveyed to the liquefied gas carrier ship 40, thereby reducing the amount of boil-off gas to be treated in the floating power generation system. In addition, it is possible to maintain the pressure of the liquefied gas storage tank of the liquefied gas carrier ship 40 can be lowered by loading the liquefied gas into the storage tank 30. Optionally, the boil-off gas conveying unit 6000 may not be provided.
  • the boil-off gas conveying unit 6000 includes a conveying line 6100.
  • the conveying line 6100 is provided such that a part of the boil-off gas generated in the storage tank 30 is conveyed to the liquefied gas carrier 40.
  • the conveying line 6100 may be provided to connect a region between the pressure control valve 5210 and the compression unit 3700 of the boil-off gas supply line 3600 and the liquefied gas carrier line 40.
  • the boil-off gas conveying unit 6000 may further include a conveying gas pressurizer 6200, a bypass line 6300, and a pressure regulating member 6400.
  • the carrier gas pressurizer 6200 pressurizes the boil-off gas in the carrier line 6100 toward the liquefied gas carrier line 40. If the pressure in the storage tank 30 is not sufficient to easily transport the boil-off gas through the transfer line 6100 to the liquefied gas carrier 40, by applying pressure to the boil-off gas by the carrier gas pressurizer 6200 The boil-off gas may be more easily conveyed to the liquefied gas carrier through the transfer line 6100.
  • the bypass line 6300 is provided such that the boil-off gas is bypassed from the storage tank 30 to the liquefied gas carrier 40 by bypassing the carrier gas pressurizer 6200.
  • the bypass line 6300 has a point where both ends are branched from the boil-off gas supply line 3600 of the conveying line 6100 and a region between the conveying gas pressurizer 6200 and the conveying gas pressurizer of the conveying line 6100. And an area between the 6200 and the liquefied gas carrier 40. If the pressure in the storage tank 30 is sufficient to easily transport the boil-off gas through the conveying line 6100 to the liquefied gas carrier 40, the boil-off gas passing through the conveying line 6100 passes through the bypass line 6300. Unnecessary energy consumption can be reduced by being conveyed to the liquefied gas carrier 40 and preventing the conveying gas pressurizer 6200 from operating unnecessarily.
  • the pressure regulating member 6400 adjusts the pressure of the liquefied gas storage tank of the liquefied gas carrier ship 40.
  • the pressure adjusting member 6400 both ends so that some of the boil-off gas pressurized by the carrier gas pressurizer 6200 is transferred to the recondensation unit 3100 through the boil-off gas supply line 3600.
  • the boil-off gas supply line 3600 and the transfer line 6100 may be provided as a valve 6400 for adjusting the opening rate of the gas line.
  • the boil-off gas conveying unit 6000 may further include a pressure measurer 6500 that measures the pressure of the carrier tank of the liquefied gas carrier.
  • the controller 5300 may adjust the pressure of the carrier tank by controlling the valve 6400 according to the pressure of the carrier tank measured by the pressure gauge 6500. By adjusting the pressure by the valve 6400, it is possible to prevent the pressure inside the carrier tank from excessively rising.
  • Other configurations, structures and functions of the fuel gas supply system shown in FIG. 7 are similar to those of the fuel gas supply system of FIG. 6.
  • the gas supply module 3000a may further include an excess gas supply unit 3800.
  • the excess gas supply unit 3800 compresses a portion of the boil-off gas in the boil-off gas supply line 3600 and supplies the compressed gas to the gas turbine 2100.
  • the excess gas supply unit 3800 includes an excess gas supply line 3810 and an excess gas compressor 3820.
  • both ends of the excess gas supply pipe 3810 may be connected to an area between the boil-off gas supply line 3600 and the gas turbine 2100 and the vaporizer 3300 of the demand supply line 3200.
  • the compression unit 3700 When the compression unit 3700 is provided, one end connected to the boil-off gas supply line 3600 of the excess gas supply pipe 3810 is connected to the compression unit 3700 and the pressure control valve 5210 of the boil-off gas supply line 3600. Is connected to the area between.
  • the excess gas compressor 3820 compresses some of the boil-off gas in the boil-off gas supply line 3600 to a pressure that can be used for the gas turbine 2100.
  • the excess gas compressor 3820 is installed in the excess gas supply pipe 3810.
  • the controller 5300 is the amount of the boil-off gas generated in the storage tank 30 exceeds the amount that can be condensed in the recondensation unit 3100, the above in the boil-off gas supply line 3600 Excess amount of evaporated gas is compressed to open the excess gas supply pipe 3810 to be mixed with the liquefied gas vaporized in the vaporizer 3300 and supplied to the gas turbine 2100, and to control the excess gas compressor 3820 to operate. .
  • the boil-off gas conveying unit 6000 of the fuel gas supply system illustrated in FIG. 8 may have a conveying gas pressurizer 6200, a bypass line 6300, a pressure regulating member 6400, and a pressure as in the fuel gas supply system of FIG. 7. It may further include a meter (5220).
  • the fuel gas supply system according to the embodiment of the present invention can reduce the amount of generated boil-off gas by cooling and pressurizing the storage tank.
  • the fuel gas supply system according to the embodiment of the present invention may utilize a large amount of boil-off gas by conveying a portion of the boil-off gas to the liquefied gas carrier or directly supplying the compressed gas to the gas turbine.
  • the floating power generation system includes a storage tank 1000, a gas power generation module 2000, a gas supply module 3000, and a circulation module 4000.
  • the liquefied gas is stored in the storage tank 1000.
  • the storage tank 1000 corresponds to a storage unit accommodating liquefied gas and its boiled gas.
  • the gas power generation module 2000 generates electricity using the liquefied gas supplied from the storage tank 1000.
  • the gas power generation module 2000 includes a gas turbine 2100 and an air cooler 2200.
  • the gas turbine 2100 generates electricity by burning a liquefied gas supplied in a gaseous state from the storage tank 1000 to rotate a turbine.
  • the air cooler 2200 cools external air introduced to the gas turbine 2100 for combustion of the liquefied gas. As the temperature of the air flowing into the gas turbine is lowered, the mass of air supplied to the gas turbine for the same time increases, thereby increasing the output of the gas turbine.
  • the gas power generation module 2000 may further include a bypass tube 2300.
  • the bypass tube 2300 is provided so that outside air flows bypass the air cooler 2200.
  • the air cooler 2200 may not be selectively provided.
  • the gas supply module 3000 supplies the liquefied gas stored in the storage tank 1000 to the gas turbine 2100.
  • the gas supply module 3000 has a vaporizer 3300.
  • the vaporizer 3300 vaporizes the liquefied gas before it is supplied to the gas turbine 2100 so that it can be used as fuel in the gas turbine 2100.
  • a compression unit 200 of FIGS. 1 to 5, or 3700 of FIGS. 6 to 8
  • a recondensation unit FIGGS. 1 to 5
  • Reference numeral 300 of FIG. 6, or reference numeral 3100 of FIGS. 6 to 8 may be provided.
  • the gas supply module 3000 may further include a gas temperature controller 3900.
  • the gas temperature controller 3900 heats the liquefied gas vaporized in the vaporizer 3300 to a temperature at which the efficiency of the gas turbine 2100 is optimized and supplies the gas turbine 2100 to the gas turbine 2100. .
  • the circulation module 4000 circulates the cooling fluid.
  • the circulation module 4000 includes a main circulation module 4100 and an auxiliary circulation module 4200.
  • the main circulation module 4100 circulates the cooling fluid to cool the cooling target 7000 which requires cooling during configuration of the floating body and / or the floating power generation system.
  • the cooling target 7000 is a general configuration requiring cooling of the floating body or the floating power generation system, and does not include the air cooler 2200 in which the cooling fluid is circulated by the auxiliary cooling module to be described below.
  • the cooling target 7000 may be a cooling facility of a ship provided as a floating body, a cooling device of various electrical equipment, or the like.
  • the main circulation module 4100 includes a cooling unit 4110, a main circulation pipe 4120, and a main pump 4130.
  • the cooling unit 4110 cools the heated cooling fluid by cooling the cooling target 7000.
  • the cooling unit 4110 may use seawater or river with a floating body as a cooling source for cooling the cooling fluid.
  • the main circulation pipe 4120 is provided as a flow path through which cooling fluid is circulated between the cooling unit 4110 and the cooling target 7000.
  • the main pump 4130 applies pressure to the cooling fluid so that the cooling fluid flows along the main circulation pipe 4120.
  • the auxiliary circulation module 4200 branches the cooling fluid circulated by the main circulation module 4100 to circulate the cooling fluid so that the cooling fluid flows into the vaporizer 3300 and the air cooler 2200.
  • the cooling fluid introduced into the vaporizer 3300 by the auxiliary circulation module 4200 exchanges heat with the liquefied gas.
  • the liquefied gas heat-exchanged with the cooling fluid in the vaporizer 3300 is vaporized to be used as fuel in the gas turbine 2100.
  • the auxiliary circulation module 4200 circulates the cooling fluid so that the cooling fluid having completed the heat exchange with the liquefied gas in the vaporizer 3300 flows into the air cooler 2200 to exchange heat with the outside air.
  • the external air heat exchanged with the cooling fluid in the air cooler 2200 is cooled before being supplied to the gas turbine 2100.
  • the cooling fluid is used as a heat source in the vaporizer 3300 to be cooled to a temperature sufficient to cool the outside air in the air cooler 2200.
  • the auxiliary circulation module 4200 includes a temperature control unit 4210.
  • the temperature control unit 4210 adjusts the temperature of the cooling fluid flowing into the vaporizer 3300.
  • the air cooler 2200 since the cooling fluid passes sequentially through the vaporizer 3300 and the air cooler 2200, the higher the temperature of the cooling fluid supplied to the vaporizer 3300, the air cooler 2200.
  • the temperature of the cooling fluid supplied to the furnace is also increased. Therefore, when the temperature of the cooling fluid flowing into the air cooler 2200 becomes higher than a predetermined temperature, the external air supplied to the gas turbine 2100 may not be sufficiently cooled.
  • the temperature control unit 4210 for adjusting the temperature of the cooling fluid flowing into the vaporizer 3300, by adjusting the temperature of the cooling fluid flowing into the vaporizer 3300 to a suitable range of temperature, the vaporizer 3300 ) The amount of cooling fluid supplied per hour and the temperature of the air cooled in the air cooler 2200 can be adjusted to an appropriate range.
  • the temperature control unit 4210 includes a mixing member 4211 and a controller 4212.
  • FIG. 10 is a block diagram illustrating the temperature control unit of FIG. 9. 9 and 10, in the mixing member 4211, the first fluid, the second fluid, and the third fluid are mixed. Cooling fluid mixed in the mixing member 4211 flows sequentially through the vaporizer 3300 and the air cooler 2200.
  • the first fluid is a cooling fluid flowing from the cooling unit 4110 to the cooling target 7000. That is, the first fluid is branched from the region in which the cooling fluid flows from the cooling unit 4110 of the main circulation pipe 4120 to the cooling target 7000 and flows into the mixing member 4211.
  • the second fluid is a cooling fluid flowing from the cooling target 7000 to the cooling unit 4110.
  • the second fluid is branched from the region where the cooling fluid flows from the cooling target 7000 of the main circulation pipe 4120 to the cooling unit 4110 and flows into the mixing member 4211.
  • the third fluid is a cooling fluid in which heat exchange with liquefied gas is completed in the vaporizer 3300.
  • the third fluid is a cooling fluid after the heat exchange in the vaporizer 3300 before passing through the bypass passage 4220 or the air cooler 2200 to the cooling target 7000 to be described below.
  • the temperature of the third fluid heat-exchanged with the liquefied gas in the liquid state is generally lower than the temperature of the second fluid heat-exchanged with the refrigerant such as seawater used in the cooling unit 4110, The temperature is higher than the temperature of the second fluid cooled in the cooling unit.
  • the controller 4212 controls the mixing member 4211 to adjust the mixing ratio between the first fluid, the second fluid, and the third fluid, in accordance with the temperature of the cooling fluid and the temperature of the external air introduced into the vaporizer 3300.
  • the temperature control unit 4210 may further include an outside air temperature measurer 4213, a cooling fluid temperature measurer 4214, and a flow rate measurer 4215.
  • the outside air temperature meter 4213 measures the temperature of the outside air of the floating body and the floating power generation system.
  • the cooling fluid temperature measuring device 4214 measures the temperature of the cooling fluid flowing into the vaporizer 3300 after being mixed in the mixing member 4211.
  • the flow meter 4215 measures the flow rate of the cooling fluid flowing into the vaporizer 3300 after mixing in the mixing member 4211.
  • the controller 4212 controls the mixing member 4211 according to the values measured at the outside air temperature meter 4213, the cooling fluid temperature meter 4214, and the flow rate meter 4215.
  • the controller 4212 may adjust the flow rate of the cooling fluid flowing into the vaporizer 3300 according to the temperature of the outside air and the temperature of the cooling fluid flowing into the vaporizer.
  • a flow regulating valve 4216 is provided for adjusting the flow rate in a flow path through which the cooling fluid mixed by the mixing member 4211 flows to the vaporizer 3300, and the controller 4212 is provided with a temperature of the outside air and a vaporizer ( When it is necessary to increase the amount of cooling fluid to be introduced into the vaporizer 3300 in accordance with the temperature of the cooling fluid introduced into the 3300, the flow control valve 4216 is controlled to increase the opening rate of the flow control valve 4216.
  • the flow control valve 4216 opens.
  • the flow control valve 4216 is controlled to lower the rate.
  • the secondary circulation module 4200 may further include a bypass flow path 4220.
  • Bypass flow path 4220 is provided to allow cooling fluid to bypass the air cooler. For example, when the temperature of the outside air sucked into the air cooler 2200 is sufficiently low so that no separate cooling is required, the cooling fluid passing through the vaporizer 3300 is not introduced into the air cooler 2200 and bypassed.
  • the cooling object 7000 is supplied to the cooling target 7000 through the flow path 4220.
  • the auxiliary circulation module 4200 circulates the cooling fluid such that the cooling fluid passing through the air cooler 2200 or the bypass flow path 4220 is mixed with the first fluid and supplied to the cooling target 7000.
  • FIG. 11 shows a fuel gas supply system according to a seventh embodiment of the present invention.
  • the temperature control unit 4210 may not be provided.
  • the cooling fluid is provided to sequentially circulate the cooling target 7000, the cooling unit 4110, and the vaporizer 3300. That is, only the first fluid flows into the vaporizer 3300.
  • Other configurations, structures and functions of the fuel gas supply system shown in FIG. 11 are similar to those of the floating power generation system of FIG. 9.
  • FIG. 12 shows a fuel gas supply system according to an eighth embodiment of the present invention.
  • FIG. 13 is a block diagram illustrating the temperature control unit of FIG. 12. 12 and 13, unlike in the case of FIG. 11, in order to further increase the temperature of the cooling fluid supplied to the vaporizer 3300, a portion of the first fluid and the second fluid provided at a higher temperature than the first fluid. Temperature control unit 4210 may be provided to mix the. In this case, a configuration for introducing the third fluid, which is provided to lower the temperature of the cooling fluid, further into the mixing member 4211 may not be provided.
  • Other configurations, structures, and functions of the fuel gas supply system shown in FIGS. 12 and 13 are similar to those of the floating power generation system of FIG. 9.
  • the fuel gas supply system shown in FIG. 14 causes the intermediate fruit to circulate in the auxiliary circulation module 4200 of the circulation module 4000, and the cooling fluid flowing in the main circulation module 4100 and the intermediate flow in the auxiliary circulation module 420.
  • the fruit is heat-exchanged by the heater 4300 and in the vaporizer 3300 by using the heat energy of the intermediate fruit of the auxiliary circulation module 4200 heated in the heater 4300 through heat exchange with the cooling fluid of the main circulation module 4100.
  • the circulation module is configured to vaporize the liquefied gas.
  • a fluid such as seawater, river water, or glycol may be used.
  • the circulation module 4000 includes a main circulation module 4100, an auxiliary circulation module 4200, and a heater 4300. Some of the cooling fluid whose temperature has risen in the process of cooling the cooling target 7000 in the main circulation module 4100 is supplied to the cooling unit 4110 and cooled, and the other part of the heater 4300 through the transfer line L80. Is transferred to. The cooling fluid transferred to the heater 4300 through the transfer line L80 is cooled in the process of heat exchange with the intermediate fruit circulating in the auxiliary circulation module 4200, and then again cooled through the main pump 4130. Supplied by.
  • the intermediate fruit circulating in the auxiliary circulation module 4200 is heat-exchanged with the cooling fluid of the main circulation module 4100 in the heater 4300 and is heated by the opposite feed to cool the cooling fluid of the main circulation module 4100.
  • the intermediate fruit heated to the heater 4300 is supplied to the vaporizer 3300 through the intermediate fruit pipe L70 by the circulation pump 4230.
  • the liquefied gas is vaporized by the heat energy of the intermediate fruit in the vaporizer 3300, and, on the contrary, the intermediate fruit is cooled by the liquefied gas and then supplied to the air cooler 2200.
  • the intermediate fruit cooled by the vaporizer 3300 cools the outside air to be supplied to the gas turbine 2100 in the air cooler 2200, and then is supplied to the heater 4300 through the intermediate heating line L50, and then again to the heater 4300. ) Is heated in the process of heat exchange with the cooling fluid of the main circulation module 4100 and is supplied to the vaporizer 3300.
  • the temperature control unit 4210 of the auxiliary circulation module 4200 adjusts the temperature of the intermediate fruit flowing into the vaporizer 330.
  • the temperature regulating unit 4210 includes a bypass pipe L60, a regulating valve 4217, and a controller 4212.
  • the bypass tube (L60) is connected to the intermediate fruit line (L50) so that the intermediate fruit flows bypass the heater (4300).
  • the control valve 4217 controls the flow rate of the intermediate fruit which bypasses the bypass pipe L60.
  • the control valve 4217 may be provided as a three-way valve installed at the contact between the intermediate fruit line (L50) and the bypass pipe (L60).
  • the control valve 4217 may be provided as a valve installed in the intermediate fruit line L50 and / or the bypass pipe L60.
  • the controller 4212 controls the regulating valve 4217 according to the temperature of the outside air measured by the outside air temperature meter 4213 and the vaporizer inlet-side medium fruit temperature measured by the middle fruit temperature meter 4214. 4300) to adjust the flow rate of the intermediate fruit.
  • the fuel gas supply system of the present invention can adjust the temperature of the heat source flowing into the vaporizer by providing a temperature control unit.
  • the fuel gas supply system of the present invention does not provide a system for circulating a separate thermal fluid or refrigerant for vaporizing liquefied gas or cooling the air supplied to the gas turbine, but instead of a cooling fluid circulated by the existing cooling module. By using it, cooling and heating efficiency can be improved.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • General Engineering & Computer Science (AREA)
  • Ocean & Marine Engineering (AREA)
  • Architecture (AREA)
  • Civil Engineering (AREA)
  • Structural Engineering (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

La présente invention concerne un système d'alimentation en gaz combustible. Un système d'alimentation en gaz combustible selon un mode de réalisation de la présente invention comprend : une unité de stockage destinée à recevoir un gaz liquéfié et un gaz vaporisé généré à partir de ce dernier; une unité de compression destinée à mettre sous pression le gaz vaporisé généré dans l'unité de stockage et à distribuer un gaz vaporisé sous pression; une unité de recondensation destinée à recondenser le gaz vaporisé mis sous pression dans l'unité de compression à l'aide d'un gaz liquéfié en surfusion de l'unité de stockage; une unité de pompe à haute pression, installée sur une ligne d'alimentation de consommateur reliant l'unité de recondensation et un consommateur, destinée à mettre sous pression un gaz liquéfié de l'unité de recondensation à une pression égale ou supérieure à une pression demandée par le consommateur; et une unité d'échange de chaleur comprenant un vaporisateur destiné à revaporiser le gaz liquéfié sous pression dans l'unité de pompe à haute pression par chauffage. L'unité de recondensation comprend : une première unité de condensation destinée à mélanger le gaz liquéfié délivré à partir de l'unité de stockage et le gaz vaporisé mis sous pression dans l'unité de compression pour recondenser le gaz vaporisé; et une seconde unité de condensation destinée à permettre au gaz liquéfié, qui a été mis sous pression dans l'unité de pompe à haute pression et ensuite distribué, et au gaz vaporisé mis sous pression dans l'unité de compression d'échanger de la chaleur l'un avec l'autre pour recondenser le gaz vaporisé.
PCT/KR2017/015736 2017-01-02 2017-12-29 Système d'alimentation en gaz combustible WO2018124815A1 (fr)

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CN201780082063.8A CN110167837B (zh) 2017-01-02 2017-12-29 燃料气体供应系统
SG11201906121RA SG11201906121RA (en) 2017-01-02 2017-12-29 Fuel gas supply system
JP2019556779A JP6876826B2 (ja) 2017-01-02 2017-12-29 燃料ガス供給システム

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KR1020170000153A KR101824421B1 (ko) 2017-01-02 2017-01-02 연료가스 공급 시스템
KR10-2017-0000153 2017-01-02
KR10-2017-0005978 2017-01-13
KR1020170005978A KR20180083556A (ko) 2017-01-13 2017-01-13 부유식 발전 시스템
KR10-2017-0005975 2017-01-13
KR1020170005975A KR101924535B1 (ko) 2017-01-13 2017-01-13 부유식 발전 시스템

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Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116626217A (zh) * 2023-04-23 2023-08-22 北京航天试验技术研究所 一种高温燃气采集装置及方法

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113734352A (zh) * 2021-09-24 2021-12-03 上海外高桥造船有限公司 一种具有再冷凝功能的供气系统和工作方法

Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20080097141A (ko) * 2007-04-30 2008-11-04 대우조선해양 주식회사 인-탱크 재응축 수단을 갖춘 부유식 해상 구조물 및 상기부유식 해상 구조물에서의 증발가스 처리방법
KR20100129039A (ko) * 2009-05-29 2010-12-08 삼성중공업 주식회사 스프레이 노즐을 구비하는 선박
KR20150057684A (ko) * 2013-11-20 2015-05-28 대우조선해양 주식회사 Lng 극저온 에너지 활용시스템 및 초대형 부유식 구조물
KR20150104668A (ko) * 2014-03-05 2015-09-16 현대중공업 주식회사 엔진 폐열을 이용한 흡기 냉각 제어시스템
KR20160062786A (ko) * 2014-11-25 2016-06-03 삼성중공업 주식회사 재액화 시스템
KR20160128662A (ko) * 2015-04-29 2016-11-08 대우조선해양 주식회사 Flng의 lng 하역 시스템 및 방법
KR101683158B1 (ko) * 2014-07-30 2016-12-07 삼성중공업 주식회사 연료 공급 시스템

Family Cites Families (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH09162933A (ja) * 1995-12-11 1997-06-20 Jatco Corp 制御装置用通信装置
US6745576B1 (en) * 2003-01-17 2004-06-08 Darron Granger Natural gas vapor recondenser system
US8499569B2 (en) * 2004-09-13 2013-08-06 Argent Marine Management, Inc. System and process for transporting LNG by non-self-propelled marine LNG carrier
US20070001322A1 (en) * 2005-06-01 2007-01-04 Aikhorin Christy E Method and apparatus for treating lng
CN101881549B (zh) * 2010-06-25 2014-02-12 华南理工大学 一种液化天然气接收站蒸发气体再冷凝回收系统及其回收方法
KR101258934B1 (ko) * 2010-12-09 2013-04-29 삼성중공업 주식회사 선박
JP5611476B2 (ja) * 2011-03-11 2014-10-22 デウ シップビルディング アンド マリーン エンジニアリング カンパニー リミテッド 再液化装置及び高圧天然ガス噴射エンジンを有する海上構造物の燃料供給システム
CN104321581B (zh) * 2011-12-02 2016-10-19 氟石科技公司 Lng蒸发气体再冷凝配置和方法
US20130298572A1 (en) * 2012-05-09 2013-11-14 Fluor Technologies Corporation Configurations and methods of vapor recovery and lng sendout systems for lng import terminals
KR101386543B1 (ko) * 2012-10-24 2014-04-18 대우조선해양 주식회사 선박의 증발가스 처리 시스템
JP2014142021A (ja) * 2013-01-24 2014-08-07 Ihi Corp タンク設備及び低温液化ガス払出方法
CN203100350U (zh) * 2013-02-07 2013-07-31 中国寰球工程公司 一种蒸发气的液化系统
CN104034122B (zh) * 2013-03-04 2016-02-10 中国石化工程建设有限公司 一种液化天然气蒸发气再冷凝系统及方法
CN203248991U (zh) * 2013-04-22 2013-10-23 中国海洋石油总公司 一种lng接收站利用压力能的bog处理系统
KR101707500B1 (ko) * 2013-10-31 2017-02-16 대우조선해양 주식회사 증발가스 처리 시스템 및 방법
KR101788749B1 (ko) * 2014-02-24 2017-10-20 대우조선해양 주식회사 증발가스 처리 시스템 및 방법
JP6404169B2 (ja) * 2015-04-02 2018-10-10 株式会社神戸製鋼所 圧縮機ユニットおよびガス供給装置
CN204717340U (zh) * 2015-06-02 2015-10-21 中国石油化工股份有限公司 一种液化天然气接收站天然气输出系统

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR20080097141A (ko) * 2007-04-30 2008-11-04 대우조선해양 주식회사 인-탱크 재응축 수단을 갖춘 부유식 해상 구조물 및 상기부유식 해상 구조물에서의 증발가스 처리방법
KR20100129039A (ko) * 2009-05-29 2010-12-08 삼성중공업 주식회사 스프레이 노즐을 구비하는 선박
KR20150057684A (ko) * 2013-11-20 2015-05-28 대우조선해양 주식회사 Lng 극저온 에너지 활용시스템 및 초대형 부유식 구조물
KR20150104668A (ko) * 2014-03-05 2015-09-16 현대중공업 주식회사 엔진 폐열을 이용한 흡기 냉각 제어시스템
KR101683158B1 (ko) * 2014-07-30 2016-12-07 삼성중공업 주식회사 연료 공급 시스템
KR20160062786A (ko) * 2014-11-25 2016-06-03 삼성중공업 주식회사 재액화 시스템
KR20160128662A (ko) * 2015-04-29 2016-11-08 대우조선해양 주식회사 Flng의 lng 하역 시스템 및 방법

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN116626217A (zh) * 2023-04-23 2023-08-22 北京航天试验技术研究所 一种高温燃气采集装置及方法
CN116626217B (zh) * 2023-04-23 2023-10-03 北京航天试验技术研究所 一种高温燃气采集装置及方法

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CN110167837B (zh) 2021-12-24
JP2020514649A (ja) 2020-05-21

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