CN111623232B - BOG and LNG cold energy comprehensive recycling system and process - Google Patents

BOG and LNG cold energy comprehensive recycling system and process Download PDF

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Publication number
CN111623232B
CN111623232B CN202010481025.3A CN202010481025A CN111623232B CN 111623232 B CN111623232 B CN 111623232B CN 202010481025 A CN202010481025 A CN 202010481025A CN 111623232 B CN111623232 B CN 111623232B
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bog
lng
working medium
mixed working
cold energy
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CN111623232A (en
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徐文东
李璋怡
张琳
何智辉
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South China University of Technology SCUT
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South China University of Technology SCUT
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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
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01B—MACHINES OR ENGINES, IN GENERAL OR OF POSITIVE-DISPLACEMENT TYPE, e.g. STEAM ENGINES
    • F01B23/00—Adaptations of machines or engines for special use; Combinations of engines with devices driven thereby
    • F01B23/10—Adaptations for driving, or combinations with, electric generators
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F02—COMBUSTION ENGINES; HOT-GAS OR COMBUSTION-PRODUCT ENGINE PLANTS
    • F02C—GAS-TURBINE PLANTS; AIR INTAKES FOR JET-PROPULSION PLANTS; CONTROLLING FUEL SUPPLY IN AIR-BREATHING JET-PROPULSION PLANTS
    • F02C6/00—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use
    • F02C6/18—Plural gas-turbine plants; Combinations of gas-turbine plants with other apparatus; Adaptations of gas-turbine plants for special use using the waste heat of gas-turbine plants outside the plants themselves, e.g. gas-turbine power heat plants
    • 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
    • F17C13/002—Details of vessels or of the filling or discharging of vessels for vessels under pressure
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17D—PIPE-LINE SYSTEMS; PIPE-LINES
    • F17D1/00—Pipe-line systems
    • F17D1/02—Pipe-line systems for gases or vapours
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17D—PIPE-LINE SYSTEMS; PIPE-LINES
    • F17D3/00—Arrangements for supervising or controlling working operations
    • F17D3/01—Arrangements for supervising or controlling working operations for controlling, signalling, or supervising the conveyance of a product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F23—COMBUSTION APPARATUS; COMBUSTION PROCESSES
    • F23J—REMOVAL OR TREATMENT OF COMBUSTION PRODUCTS OR COMBUSTION RESIDUES; FLUES 
    • F23J15/00—Arrangements of devices for treating smoke or fumes
    • F23J15/06—Arrangements of devices for treating smoke or fumes of coolers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/16—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being arranged in parallel spaced relation
    • 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
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/03—Treating the boil-off
    • F17C2265/032—Treating the boil-off by recovery
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/06—Fluid distribution
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/07—Generating electrical power as side effect
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/14—Combined heat and power generation [CHP]
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E20/00—Combustion technologies with mitigation potential
    • Y02E20/30—Technologies for a more efficient combustion or heat usage

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Chemical & Material Sciences (AREA)
  • Combustion & Propulsion (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Abstract

The invention discloses a BOG and LNG cold energy comprehensive recycling system and process, wherein the system comprises a BOG condensation regasification system, a BOG direct compression output system, a BOG cogeneration system and an LNG cold energy power generation system; the BOG condensation regasification system comprises an LNG storage tank, an LNG immersed pump, an LNG booster pump, a BOG buffer tank, a BOG compressor of the condensation regasification system, a pressurized LNG-BOG precooler and a BOG recondenser; the BOG direct compression and output system comprises a BOG seawater preheater, an external transmission system BOG compressor and a BOG seawater cooler; the BOG cogeneration system comprises a thermoelectric system BOG compressor, BOG pressure regulating and metering equipment, a first gas turbine generator set, a flue gas waste heat boiler and a second gas turbine generator set; the invention is suitable for BOG recovery systems under different working conditions, and solves the problem of difficult recovery due to overlarge fluctuation of BOG production.

Description

BOG and LNG cold energy comprehensive recycling system and process
Technical Field
The invention belongs to the field of comprehensive energy recycling of LNG (liquefied natural gas) receiving stations, and particularly relates to a BOG and LNG cold energy comprehensive recycling system and process.
Background
Up to half 2019, 21 LNG stations built at home have been put into production, but cold energy generated in the LNG receiving and discharging process is not well utilized. Meanwhile, a large amount of BOG (LNG evaporation gas) can be generated in the operation process of the LNG receiving station, good recycling cannot be achieved, only a small part of BOG (flash evaporation gas) is recycled at present, and most of BOG is burnt and discharged through a torch system, so that energy waste is caused. These two parts result in a great degree of energy waste, which in turn results in great economic losses. Therefore, the design of a proper LNG cold energy utilization and BOG recycling method has important significance.
The publication number is CN109386316A, and the name is Chinese patent document of a LNG cold energy and BOG combustion energy combined utilization system and method, which discloses a LNG cold energy and BOG combined utilization system, high-temperature steam generated by BOG combustion generates electricity through a generator, one part of waste heat steam is used for heating a circulating medium cooled by LNG, and the other part of waste heat steam provides heat energy for a heat supply subsystem, so that the purpose of improving the power generation efficiency of the system is achieved. However, this technique is limited to the load range of the BOG gas turbine, and has low flexibility, and cannot be used for very good treatment when the BOG load of the LNG receiving station fluctuates greatly.
Chinese patent document with publication number CN109404079a, entitled BOG recondensing and LNG cold energy power generation integrated system for LNG receiving station, discloses a method for using LNG cold energy power generation for BOG recondensing process. However, the low-temperature Rankine cycle cold energy is low in efficiency for converting the cold energy into the electric energy, so that the method is not high in utilization efficiency.
Therefore, a process is needed which has high energy recovery rate and high operation flexibility and can well cope with the fluctuation of the BOG load of the LNG receiving station, and the cold energy and the generated BOG of the LNG receiving station are recovered. The process takes a peak regulation type LNG receiving station as an example, skillfully combines LNG cold energy utilization with BOG recycling, takes the fact that BOG production amount in different periods is greatly fluctuated, adopts condensation regasification, combustion power generation and direct compression processes to cooperatively recycle BOG, and simultaneously utilizes flue gas waste heat generated after BOG combustion power generation to generate hot water to provide a heat source for LNG cold energy power generation, so that the process has strong cooperativity and good operation elasticity, and reduces BOG waste while LNG cold energy power generation is fully realized.
Disclosure of Invention
Aiming at the problem that BOG and LNG cold energy generated in the operation process of the LNG receiving station are not well recycled, the invention provides a BOG and LNG cold energy recycling process suitable for the LNG receiving station, so that the collaborative recycling of residual energy of the LNG receiving station is achieved, and the energy utilization rate of the LNG receiving station is improved. According to the different LNG external transmission quantity and BOG production quantity in the LNG receiving station base load non-ship unloading period, the base load ship unloading period, the peak shaving non-ship unloading period and the peak shaving ship unloading period, the condensation regasification, the combustion power generation and the direct compression process are respectively arranged to cooperatively recycle BOG, and meanwhile, the flue gas waste heat generated after BOG combustion power generation is utilized to generate hot water to provide a heat source for LNG cold energy power generation, so that the efficiency of a cold energy power generation system is improved.
The invention is realized at least by one of the following technical schemes.
A BOG and LNG cold energy comprehensive recycling system comprises a BOG condensation regasification system, a BOG direct compression output system, a BOG cogeneration system and an LNG cold energy power generation system;
The BOG condensation regasification system comprises an LNG storage tank, an LNG immersed pump, an LNG booster pump, a BOG buffer tank, a BOG compressor of the condensation regasification system, a pressurized LNG-BOG precooler and a BOG recondenser which are connected with the LNG booster pump; the LNG storage tank, the BOG buffer tank, the BOG compressor of the condensation regasification system, the pressurized LNG-BOG precooler and the BOG recondenser are sequentially connected; the LNG immersed pump divides natural gas in the LNG storage tank into two streams, and the LNG booster pump and the BOG recondenser are both connected with the LNG immersed pump; the LNG pressurizing pump divides the pressurized LNG into two streams, one stream is sent to the pressurized LNG-BOG precooler to precool the BOG from the BOG buffer tank, and the other stream is mixed with the LNG sent back after precooling and then sent to the downstream external transmission and LNG cold energy power generation system;
the BOG direct compression and output system comprises a BOG seawater preheater, a BOG direct compression and output system BOG compressor and a BOG seawater cooler, wherein the BOG seawater preheater, the BOG direct compression and output system BOG compressor and the BOG seawater cooler are connected with the BOG buffer tank; the BOG seawater preheater, the BOG direct compression output system BOG compressor and the BOG seawater cooler are connected in sequence;
The BOG cogeneration system comprises a thermoelectric system BOG compressor, BOG pressure regulating and metering equipment, a first gas turbine generator set, a flue gas waste heat boiler and a second gas turbine generator set, wherein the thermoelectric system BOG compressor is connected with the BOG seawater preheater; the BOG compressor, the BOG pressure regulating metering equipment, the first gas turbine generator set and the flue gas waste heat boiler of the thermoelectric system are connected in sequence;
The LNG cold energy power generation system comprises an LNG raw seawater gasifier, a natural gas metering system connected with the LNG raw seawater gasifier, an LNG-mixed working medium heat exchanger, an LNG seawater reheater connected with the LNG-mixed working medium heat exchanger, a mixed working medium storage tank, a mixed working medium booster pump, a mixed working medium reheater connected with a flue gas waste heat boiler and an expansion generator connected with the LNG-mixed working medium heat exchanger; the LNG-mixed working medium heat exchanger, the mixed working medium storage tank, the mixed working medium booster pump, the mixed working medium reheater and the expansion generator are connected in a lean way.
According to the utilization process of the BOG and LNG cold energy comprehensive recycling system, the BOG condensation and regasification system is characterized in that LNG in an LNG storage tank is pressurized to 4-6 bar by an LNG immersed pump at-164 to-161 ℃ and then is divided into two streams, one stream is conveyed to an LNG pressurizing pump, and the other stream enters a BOG recondenser to condense BOG;
The LNG pressurized by the LNG booster pump is divided into two streams, one stream is sent to a pressurized LNG-BOG precooler to precool the BOG from the BOG buffer tank, and the other stream is mixed with the LNG sent back after precooling and then sent to a downstream export and LNG cold energy power generation system;
Introducing BOG which is introduced from an LNG storage tank to a BOG buffer tank at the temperature of-150 ℃ and 1.15bar, introducing the BOG into the BOG buffer tank, compressing the BOG buffer tank to 4-6 bar through a BOG compressor of a condensation regasification system, wherein the pressure is consistent with the LNG pressure at an outlet of an LNG immersed pump, precooling and exchanging heat between the compressed BOG and part of LNG which is pressurized by the LNG pressurizing pump in a pressurized LNG-BOG precooler, cooling to the temperature of-100 to-90 ℃, then introducing the BOG recondenser to be in direct contact with one strand of LNG which is introduced from the LNG immersed pump for heat exchange and condensation, cooling to the temperature of-135 to-142 ℃, introducing the LNG which is introduced from the BOG recondenser to be mixed with the other strand of LNG which is introduced from the LNG immersed pump, cooling to the temperature of-138 to-145 ℃, pressurizing to 65bar, and raising the temperature to the temperature of-135 to-142 ℃, precooling part of the LNG after pressurization, and introducing the other part of the LNG into the LNG after precooling and exchanging heat to the downstream;
The BOG direct compression and output system is characterized in that BOG which is led out of an LNG storage tank enters a BOG buffer tank at-150 ℃ and 1.15bar, is preheated to-55 to-50 ℃ by a BOG seawater preheater, enters a BOG compressor of the BOG direct compression and output system, is compressed to 4bar, is cooled by a BOG seawater cooler and is then externally output to a medium-low pressure pipe network;
The BOG cogeneration system is characterized in that BOG (boil off gas) at the temperature of-150 ℃ and 1.15bar led out of an LNG (liquefied natural gas) storage tank enters a BOG buffer tank, flows through a BOG seawater preheater to be preheated to the temperature of-55 to-50 ℃, is compressed to 16-20 bar by a BOG compressor of a thermoelectric system, and enters a first gas turbine generator set and a second gas turbine generator set to generate electricity after passing through pressure regulating metering equipment; the flue gas is introduced into a flue gas waste heat boiler and exchanges heat with cold water at 25-35 ℃, and the generated hot water at 65-75 ℃ is used as a circulating heat source of an LNG cold energy power generation system;
The LNG at 65bar and minus 132 ℃ to minus 140 ℃ from the LNG booster pump is divided into two paths, one path of LNG is gasified along the LNG raw seawater gasifier and then is transmitted outwards, the other path of LNG exchanges heat with the mixed working medium through the LNG-mixed working medium heat exchanger, and the natural gas after heat exchange is heated to 0 ℃ through the LNG seawater reheater and then is sent to an output pipeline network through the natural gas metering system;
The mixed working medium is cooled to liquid state through an LNG-mixed working medium heat exchanger, enters a mixed working medium storage tank, the liquid mixed working medium from the mixed working medium storage tank is pressurized through a mixed working medium booster pump, then enters a mixed working medium reheater, is heated to gaseous state by circulating hot water generated in a flue gas waste heat boiler, enters an expansion generator for power generation, an outlet of the expansion generator is connected with a hot material flow inlet of the LNG-mixed working medium heat exchanger, and after expansion, the low-temperature low-pressure gaseous mixed working medium enters the LNG-mixed working medium heat exchanger to exchange heat with low-temperature LNG for condensation, and the temperature is reduced to be changed into liquid state to the next cycle.
Further, the mixed working medium for LNG cold energy power generation is a combination of at least two of the organic working media.
Further, the heat source for reheating the mixed working medium of the LNG cold energy power generation system is hot water generated by a flue gas waste heat boiler.
Further, a feedback regulating valve is arranged at the front LNG split flow position of the LNG-mixed working medium heat exchanger, the LNG split flow position is regulated according to fluctuation of the downstream natural gas consumption, when the natural gas demand is too large or too small, the LNG raw seawater gasifier is opened for gasification, and then the LNG raw seawater gasifier is conveyed to the downstream after pressure regulation and metering.
Furthermore, the process fully considers the fluctuation of BOG along with LNG and whether to ship unloading, and aims at four different conditions mainly existing in an LNG receiving station, namely, a base load non-ship unloading period, a peak shaving non-ship unloading period and a peak shaving ship unloading period, wherein the BOG condensation regasification system, the BOG direct compression export system and the BOG cogeneration system are utilized to process the generated BOG.
Furthermore, during the periods of the base load output and the base load non-ship unloading, the BOG production amount is minimum, and at the moment, a gas turbine is started to recycle and burn the BOG, and the condensation regasification and the compression are not adopted for medium-low pressure pipe network facilities.
Furthermore, during the period of the base load export and ship unloading, the LNG export quantity is unchanged, the BOG production quantity is increased due to the ship unloading, the exported LNG is liquefied by the BOG condensation regasification system, two gas turbines are started to recycle the BOG, and the rest BOG is treated by compressing into a pipe network.
Further, during peak regulation export and non-ship unloading periods, LNG export quantity is increased sharply, BOG production quantity is further increased, BOG processing quantity of the BOG condensation regasification system is increased along with the increase of LNG export quantity, at the moment, two gas turbines are started to recycle, burn and generate electricity and condense and regasifie BOG, and the rest BOG enters a medium-low pressure pipe network through compression.
Further, during the periods of peak regulation and ship unloading, the LNG output is increased sharply, the BOG production is maximum, at the moment, the BOG condensation and regasification system, the BOG direct compression output system and the BOG cogeneration system are started at full load, and the rest BOG is combusted through a torch.
Compared with the prior art, the invention has the following beneficial effects:
1. the BOG combustion power generation system, the condensation regasification system and the compression pipe network system are used for recovering BOG, so that the process has strong cooperativity and good operation elasticity.
2. And hot water is generated by utilizing the waste heat of the flue gas after BOG combustion power generation to provide a heat source for LNG cold energy power generation, so that the waste of BOG is reduced while LNG cold energy power generation is fully realized.
3. The problem of BOG production fluctuation is too big and is retrieved difficultly is solved, LNG cold energy generating efficiency and receiving station's energy utilization rate have been improved.
Drawings
FIG. 1 is a schematic diagram of a comprehensive BOG and LNG cold energy recycling process according to an embodiment of the invention;
The figure shows: the system comprises a 1-LNG storage tank, a 2-LNG immersed pump, a 3-LNG booster pump, a 4-LNG raw seawater gasifier, a 5-natural gas metering system, a 6-BOG buffer tank, a 7-condensation regasification system BOG compressor, an 8-supercharging LNG-BOG precooler, a 9-BOG recondenser, a 10-BOG seawater preheater, an 11-BOG direct compression export system BOG compressor, a 12-BOG seawater cooler, a 13-LNG-mixed working medium heat exchanger, a 14-LNG seawater reheater, a 15-mixed working medium storage tank, a 16-mixed working medium booster pump, a 17-mixed working medium reheater, an 18-expansion generator, a 19-thermoelectric system BOG compressor, a 20-BOG pressure regulating metering device, a 21-smoke waste heat boiler, a 22-first gas turbine generator set and a 23-second gas turbine generator set.
Detailed Description
For a better understanding of the present invention, reference will now be made to the following description of the invention taken in conjunction with the accompanying drawings and examples, which are included to illustrate and not limit the scope of the invention.
The construction scale of a certain peak regulation type LNG receiving station is 500 multiplied by 10 4 t/a, the LNG output base load is kept at 150 multiplied by 10 4Sm3/d (namely 45 t/h), the peak regulation output quantity is 1800 multiplied by 10 4Sm3/d (namely 585 t/h), the LNG output storage tank temperature is-161 ℃, and the gasification pressure is 8MPa. The maximum gasification output capacity is 6000 x 10 4Sm3/d.
The BOG production amount is 6.12-6.36 t/h when the base load is not discharged from the ship, the BOG production amount is 22.94-23.10 t/h when the base load is discharged from the ship, the BOG production amount is 43.81-44.68 t/h when the base load is discharged from the ship, and the BOG production amount is 60.39-63.46 t/h when the base load is discharged from the ship. The station was equipped with a BOG condensing and regasification system with a throughput of 20t/h and two 9000 (12.16 t/h total throughput) BOG compressors could compress the BOG into a 0.4MPa network. In addition, the process of the invention adds two sets of gas turbine generator sets with the design scale of 6t/h to adjust the BOG recovery system.
The BOG and LNG cold energy comprehensive recycling system shown in the figure 1 comprises a BOG condensation regasification system, a BOG direct compression export system, a BOG cogeneration system and an LNG cold energy power generation system;
The BOG condensation regasification system comprises an LNG storage tank 1, an LNG immersed pump 2, an LNG booster pump 3, a BOG buffer tank 6, a condensation regasification system BOG compressor 7, a booster LNG-BOG precooler 8 and a BOG recondenser 9, wherein the booster LNG-BOG precooler 8 is connected with the LNG booster pump 3; the LNG storage tank 1, the BOG buffer tank 6, the BOG compressor 7 of the condensation regasification system, the pressurized LNG-BOG precooler 8 and the BOG recondenser 9 are connected in sequence; the LNG immersed pump 2 divides the natural gas in the LNG storage tank 1 into two parts, and the LNG booster pump 3 and the BOG recondenser 9 are connected with the LNG immersed pump 2; the LNG pressurizing pump 3 divides the pressurized LNG into two streams, one stream is sent to the pressurized LNG-BOG precooler 8 to precool the BOG from the BOG buffer tank 6, and the other stream is mixed with the LNG sent back after precooling and then sent to a downstream external transmission and LNG cold energy power generation system;
the BOG direct compression and output system comprises a BOG seawater preheater 10 connected with the BOG buffer tank 6, a BOG compressor 11 of the BOG direct compression and output system and a BOG seawater cooler 12; the BOG seawater preheater 10, the BOG direct compression output system BOG compressor 11 and the BOG seawater cooler 12 are connected in sequence;
The BOG cogeneration system comprises a thermoelectric system BOG compressor 19 connected with a BOG seawater preheater 10, BOG pressure regulating metering equipment 20, a first gas turbine generator set 22, a flue gas waste heat boiler 21 and a second gas turbine generator set 23 connected with the BOG pressure regulating metering equipment 20; the BOG compressor 19, the BOG pressure regulating metering device 20, the first gas turbine generator set 22 and the flue gas waste heat boiler 21 of the thermoelectric system are connected in sequence;
The LNG cold energy power generation system comprises an LNG raw seawater gasifier 4, a natural gas metering system 5 connected with the LNG raw seawater gasifier 4, an LNG-mixed working medium heat exchanger 13, an LNG seawater reheater 14 connected with the LNG-mixed working medium heat exchanger 13, a mixed working medium storage tank 15, a mixed working medium booster pump 16, a mixed working medium reheater 17 connected with a flue gas waste heat boiler 21 and an expansion generator 18 connected with the LNG-mixed working medium heat exchanger 13; the LNG-mixed working medium heat exchanger 13, the mixed working medium storage tank 15, the mixed working medium booster pump 16, the mixed working medium reheater 17 and the expansion generator 18 are sequentially connected.
The BOG and LNG cold energy comprehensive recycling system comprises the following process flows:
BOG condensation regasification system: LNG at-161 ℃ and 1.15bar in the LNG storage tank 1 is pressurized to 5.5bar through the LNG immersed pump 2 and is divided into two LNG streams, one LNG stream is delivered to the LNG pressurizing pump 3, and the other LNG stream enters the BOG recondenser 9 to condense BOG;
The LNG pressurized by the LNG booster pump 3 is divided into two streams, one stream is sent to a pressurized LNG-BOG precooler (8) to precool the BOG from the BOG buffer tank 6, and the other stream is mixed with the LNG sent back after precooling and then sent to a downstream external transmission and LNG cold energy power generation system;
BOG with the temperature of 150 ℃ below zero and 1.15bar is led out from the top of an LNG storage tank 1, is compressed to 5.5bar through a BOG compressor 7 of a condensation regasification system after being stabilized, is pre-cooled and exchanges heat with part of LNG pressurized by an LNG pressurizing pump 3 in a pressurized LNG-BOG precooler 8 after the temperature is increased to 67.49 ℃ below zero, is cooled to 100 ℃ below zero, is directly contacted and exchanges heat with one strand of LNG coming out of an LNG immersed pump 2 to be condensed after entering the BOG recondensor 9, is cooled to 137.65 ℃ below zero, is mixed with the other strand of LNG coming out of the LNG immersed pump 2 after coming out of the BOG recondensor 9, is cooled to 139.19 ℃ below zero, is pressurized to 65bar by entering the LNG pressurizing pump 3, and is heated to 134.76 ℃ below zero. And (3) re-precooling the BOG by a part of the pressurized LNG, and raising the mixing temperature of the other part of the pressurized LNG and the LNG at the temperature of-131.78 ℃ after precooling heat exchange to the temperature of-132.38 ℃ and then entering the downstream. The process can liquefy 1t BOG per 6.86t LNG.
BOG direct compression output system: the BOG which is led out of the LNG storage tank 1 and at the temperature of-150 ℃ and 1.15bar enters the BOG buffer tank 6, is preheated to the temperature of-55 to-50 ℃ by the BOG seawater preheater 10, then enters the BOG compressor 11 of the BOG direct compression external transmission system to be compressed to 4bar, and is cooled by the BOG seawater heat exchanger 12 and is then externally transmitted to the medium-low pressure pipeline.
The BOG cogeneration system comprises: after the BOG at the temperature of-150 ℃ and 1.15bar led out of the LNG storage tank 1 enters the BOG buffer tank 6, the BOG is preheated to the temperature of-55 ℃ by the BOG seawater preheater 10, compressed to 18bar by the thermoelectric system BOG compressor 19, enters the first gas turbine generator set 22 and the second gas turbine generator set 23 to generate electricity by the pressure regulating metering equipment 20, the tail gas is led into the flue gas waste heat boiler 21 and exchanges heat with cold water at the temperature of 30 ℃, and the generated hot water at the temperature of 70 ℃ is used as a circulating heat source of the LNG cold energy power generation system.
LNG cold energy power generation system: the 65bar LNG at the temperature of minus 132.38 ℃ coming out of the BOG condensation and regasification system is divided into two paths, one path of LNG is output outwards along the original LNG raw seawater gasifier 4 of the station, the other path of LNG exchanges heat with a mixed working medium through an LNG-mixed working medium heat exchanger 13, and the mixed working medium is C2C3 (ethane and propane mixture). After the heat exchange, the natural gas is heated to 0 ℃ by an LNG seawater reheater 14, and then passes through an original natural gas metering system 5 of an LNG receiving station, and passes through an external pipeline network of a natural gas output main pipe;
The liquid C2C3 with the temperature of-61 ℃ which is 0.2MPa and comes out of the mixed refrigerant storage tank 15 (mixed refrigerant is C2C3 in the embodiment, namely, ethane and propane are mixed) is pressurized to 1.1MPa by the mixed refrigerant booster pump 16, the temperature is increased to-60 ℃, then the mixed refrigerant is heated to 40 ℃ (gaseous state) by hot water with normal pressure and 70 ℃ which is generated in the flue gas waste heat boiler 21 by the mixed refrigerant reheater 17, and the mixed refrigerant enters the expansion generator 18 to be expanded to generate electricity, the temperature is reduced to-19 ℃ and enters the LNG-mixed refrigerant heat exchanger 13 to exchange heat, and the temperature is reduced to-61 ℃ to the next cycle. The LNG cold energy power generation system 1t LNG can generate about 20kW, and the power generation power is 16kW without hot water reheating, so that the LNG cold energy power generation system can improve the LNG cold energy power generation efficiency by about 25%.
In the periods of base load export and non-ship unloading, the LNG export quantity is 45t/h, the BOG production quantity is 6.12 t/h-6.36 t/h, and at the moment, a gas turbine can be started to burn to recover and burn the BOG without adopting condensation regasification and compression into a medium-low pressure pipe network.
During the process of base load export and ship unloading, the LNG export quantity is 45t/h, the BOG production quantity is about 23t/h, the BOG with the speed of 6.56t/h can be processed by condensation and regasification, at the moment, two gas turbines are started to burn to recycle the BOG (12 t/h), and the BOG with the speed of 4.44t/h is processed by compressing into a pipe network.
During peak-shaving export and non-ship unloading periods, the LNG export quantity is increased to 585t/h, the BOG production quantity is about 44t/h, and the BOG of 20t/h can be processed by condensation and regasification. At the moment, two gas turbines can be started to recycle, burn and generate electricity for BOG, a BOG condensation regasification system is started, and the BOG of the rest 12t/h is compressed and enters a medium-low pressure pipe network.
In the peak regulation and ship unloading periods, the LNG output is increased to 585t/h, the BOG production is 60.39-63.46 t/h, at the moment, two gas turbines can be started at full load to recycle and burn BOG to generate electricity, a BOG condensation regasification system, a BOG direct compression output system and a BOG cogeneration system are started, the residual BOG combusted flue gas is used for reheating mixed working media in an LNG cold energy power generation process by generating hot water through a flue gas waste heat boiler 21, and the LNG cold energy power generation efficiency is improved by about 25%.
The above examples of the present invention are merely illustrative of the present invention and are not intended to limit the embodiments of the present invention. Other variations or modifications of the above teachings will be apparent to those of ordinary skill in the art. It is not necessary here nor is it exhaustive of all embodiments. Any modification, equivalent replacement, improvement, etc. which come within the spirit and principles of the invention are desired to be protected by the following claims.

Claims (8)

1. BOG and LNG cold energy comprehensive recycling system, its characterized in that: the system comprises a BOG condensation and regasification system, a BOG direct compression output system, a BOG cogeneration system and an LNG cold energy power generation system;
The BOG condensation regasification system comprises an LNG storage tank (1), an LNG immersed pump (2), an LNG booster pump (3), a BOG buffer tank (6), a condensation regasification system BOG compressor (7), a pressurized LNG-BOG precooler (8) connected with the LNG booster pump (3) and a BOG recondensor (9); the LNG storage tank (1), the BOG buffer tank (6), the BOG compressor (7) of the condensation regasification system, the pressurized LNG-BOG precooler (8) and the BOG recondenser (9) are sequentially connected; the LNG immersed pump (2) divides natural gas in the LNG storage tank (1) into two parts, and the LNG booster pump (3) and the BOG recondenser (9) are connected with the LNG immersed pump (2); the LNG pressurizing pump (3) divides the pressurized LNG into two streams, one stream is sent to the pressurized LNG-BOG precooler (8) to precool the BOG from the BOG buffer tank (6), and the other stream is mixed with the LNG sent back after precooling and then sent to the downstream external transmission and LNG cold energy power generation system;
The BOG direct compression and output system comprises a BOG seawater preheater (10) connected with the BOG buffer tank (6), a BOG compressor (11) of the BOG direct compression and output system and a BOG seawater cooler (12); the BOG seawater preheater (10), the BOG direct compression output system BOG compressor (11) and the BOG seawater cooler (12) are connected in sequence;
The BOG cogeneration system comprises a thermoelectric system BOG compressor (19) connected with a BOG seawater preheater (10), BOG pressure regulating metering equipment (20), a first gas turbine generator set (22), a flue gas waste heat boiler (21) and a second gas turbine generator set (23) connected with the BOG pressure regulating metering equipment (20); the BOG compressor (19), the BOG pressure regulating metering equipment (20), the first gas turbine generator set (22) and the flue gas waste heat boiler (21) of the thermoelectric system are connected in sequence;
The LNG cold energy power generation system comprises an LNG raw seawater gasifier (4), a natural gas metering system (5) connected with the LNG raw seawater gasifier (4), an LNG-mixed working medium heat exchanger (13), an LNG seawater reheater (14) connected with the LNG-mixed working medium heat exchanger (13), a mixed working medium storage tank (15), a mixed working medium booster pump (16), a mixed working medium reheater (17) connected with a flue gas waste heat boiler (21) and an expansion generator (18) connected with the LNG-mixed working medium heat exchanger (13); the LNG-mixed working medium heat exchanger (13), the mixed working medium storage tank (15), the mixed working medium booster pump (16), the mixed working medium reheater (17) and the expansion generator (18) are sequentially connected;
The BOG condensation and regasification system comprises an LNG storage tank (1), wherein LNG of 1.15bar is pressurized to 4.6 bar by an LNG immersed pump (2) at the temperature of-164-161 ℃ and then divided into two streams, one stream is conveyed to an LNG pressurizing pump (3), and the other stream enters a BOG recondenser (9) to condense BOG;
The LNG pressurized by the LNG booster pump (3) is divided into two streams, one stream is sent to a pressurized LNG-BOG precooler (8) to precool the BOG from the BOG buffer tank (6), and the other stream is mixed with the LNG sent back after precooling and then sent to a downstream external transmission and LNG cold energy power generation system;
Introducing 1.15bar BOG which is introduced from an LNG storage tank (1) into a BOG buffer tank, introducing the BOG buffer tank (6), compressing the BOG to 4 bar by a BOG compressor (7) of a condensation and regasification system, wherein the pressure is consistent with the LNG pressure at an outlet of an LNG immersed pump (2), pre-cooling the compressed BOG and part of the pressurized LNG by an LNG pressurizing pump (3) in a pressurized LNG-BOG precooler (8), cooling to-100-90 ℃, then introducing the BOG and one strand of LNG which is introduced from the LNG immersed pump (2) into a BOG recondenser (9), directly contacting and exchanging heat and condensing the BOG and the other strand of LNG, reducing the temperature to-135-142 ℃, introducing the BOG and the other strand of LNG which is introduced from the LNG recondenser (9), reducing the temperature to-138-145 ℃, introducing the LNG pump (3) to boost the pressure to 65bar, introducing the pressurized part of the LNG and re-precooling the LNG after the pressurized LNG and the other part of the LNG after pre-pressurizing and pre-cooling into the downstream after the mixture;
The BOG direct compression and output system is characterized in that BOG which is led out of an LNG storage tank (1) enters a BOG buffer tank (6) at the temperature of-150 ℃ and 1.15bar, is preheated to the temperature of-55 to 50 ℃ by a BOG seawater preheater (10), enters a BOG direct compression and output system BOG compressor (11) to compress to 4bar, is cooled by a BOG seawater cooler (12) and is then externally output to a medium-low pressure pipe network;
The BOG cogeneration system is characterized in that BOG (boil off gas) at the temperature of-150 ℃ and 1.15bar is led out of an LNG storage tank (1) and enters a BOG buffer tank (6), and then flows through a BOG seawater preheater (10) to be preheated to the temperature of-55-50 ℃, is compressed to 16-20 bar through a BOG compressor (19) of a thermoelectric system, and enters a first gas turbine generator set (22) and a second gas turbine generator set (23) to generate electricity after passing through BOG pressure regulating metering equipment (20); the flue gas is introduced into a flue gas waste heat boiler (21) and exchanges heat with cold water at 25 ℃ and the generated hot water at 65 ℃ is used as a circulating heat source of an LNG cold energy power generation system;
the LNG cold energy power generation system is characterized in that 65bar of LNG at the temperature of minus 132-140 ℃ from the LNG booster pump (3) is divided into two paths, one path of LNG is gasified along the LNG raw seawater gasifier (4) and then is transmitted outwards, the other path of LNG exchanges heat with the mixed working medium through the LNG-mixed working medium heat exchanger (13), and the natural gas after heat exchange is heated to the temperature of 0 ℃ through the LNG seawater reheater (14) and then is sent to an external transmission pipeline network through the natural gas metering system (5);
the mixed working medium is cooled to be liquid through an LNG-mixed working medium heat exchanger (13), enters a mixed working medium storage tank (15), the liquid mixed working medium from the mixed working medium storage tank (15) is pressurized through a mixed working medium booster pump (16), then enters a mixed working medium reheater (17), is heated to be gaseous by circulating hot water generated in a flue gas waste heat boiler (21), enters an expansion generator (18) to generate electricity, an outlet of the expansion generator (18) is connected with a hot material flow inlet of the LNG-mixed working medium heat exchanger (13), and after expansion, the low-temperature low-pressure gaseous mixed working medium enters the LNG-mixed working medium heat exchanger (13) to exchange heat with low-temperature LNG for condensation, and the temperature is reduced to be liquid to the next cycle;
aiming at four different conditions mainly existing in an LNG receiving station, namely a base load non-ship unloading period, a base load ship unloading period, a peak shaving non-ship unloading period and a peak shaving ship unloading period, the BOG condensation regasification system, the BOG direct compression export system and the BOG cogeneration system are utilized to process the generated BOG.
2. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: the mixed working medium of the LNG cold energy power generation system is a combination of at least two of the organic working media.
3. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: the mixed working medium reheating heat source of the LNG cold energy power generation system is hot water generated by a flue gas waste heat boiler (21).
4. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: and a feedback regulating valve is arranged at the front LNG split flow position of the LNG-mixed working medium heat exchanger (13), the regulation is carried out according to the fluctuation of the downstream natural gas consumption, and when the natural gas demand is too large or too small, the LNG raw seawater gasifier (4) is opened for gasification and then is conveyed downstream after passing through the natural gas metering system (5).
5. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: during the period of the output of the base load and the non-ship unloading of the base load, the BOG production amount is minimum, and at the moment, a gas turbine is started to recycle and burn the BOG without adopting condensation and regasification and compression into a medium-low pressure pipe network.
6. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: during the process of base load export and ship unloading, the LNG export quantity is unchanged, the BOG production quantity is increased due to ship unloading, the exported LNG is liquefied by the BOG condensation and regasification system, two gas turbines are started to recycle the BOG, and the rest BOG is treated by compressing the BOG into a pipe network.
7. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: in the periods of peak regulation and export and non-ship unloading, the LNG export quantity is increased sharply, the BOG production quantity is further increased, along with the increase of the LNG export quantity, the BOG processing quantity of the BOG condensation regasification system is also increased, at the moment, two gas turbines are started to recycle, burn and generate electricity and condense and regasifie the BOG, and the rest BOG enters a medium-low pressure pipe network through compression.
8. The BOG and LNG cold energy comprehensive recovery and utilization system according to claim 1, wherein: in the periods of peak regulation and ship unloading, the LNG output is increased sharply, the BOG production is maximum, at the moment, a BOG condensation and regasification system, a BOG direct compression output system and a BOG cogeneration system are started at full load, and the rest BOG is combusted through a torch.
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