CN111623232A - BOG and LNG cold energy comprehensive recycling system and process - Google Patents
BOG and LNG cold energy comprehensive recycling system and process Download PDFInfo
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- CN111623232A CN111623232A CN202010481025.3A CN202010481025A CN111623232A CN 111623232 A CN111623232 A CN 111623232A CN 202010481025 A CN202010481025 A CN 202010481025A CN 111623232 A CN111623232 A CN 111623232A
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- 238000000034 method Methods 0.000 title claims abstract description 34
- 238000004064 recycling Methods 0.000 title claims abstract description 21
- 239000013535 sea water Substances 0.000 claims abstract description 52
- 238000010248 power generation Methods 0.000 claims abstract description 49
- 238000009833 condensation Methods 0.000 claims abstract description 44
- 230000005494 condensation Effects 0.000 claims abstract description 43
- 239000007789 gas Substances 0.000 claims abstract description 38
- 238000007907 direct compression Methods 0.000 claims abstract description 30
- 239000002918 waste heat Substances 0.000 claims abstract description 25
- 239000003546 flue gas Substances 0.000 claims abstract description 24
- UGFAIRIUMAVXCW-UHFFFAOYSA-N Carbon monoxide Chemical compound [O+]#[C-] UGFAIRIUMAVXCW-UHFFFAOYSA-N 0.000 claims abstract description 23
- 230000001105 regulatory effect Effects 0.000 claims abstract description 16
- 238000004519 manufacturing process Methods 0.000 claims abstract description 12
- 239000003949 liquefied natural gas Substances 0.000 claims description 236
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 claims description 34
- 239000003345 natural gas Substances 0.000 claims description 18
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 230000033228 biological regulation Effects 0.000 claims description 11
- 239000006200 vaporizer Substances 0.000 claims description 11
- 238000007906 compression Methods 0.000 claims description 6
- 230000006835 compression Effects 0.000 claims description 6
- 239000007788 liquid Substances 0.000 claims description 6
- 238000001816 cooling Methods 0.000 claims description 5
- 238000003303 reheating Methods 0.000 claims description 4
- 230000005540 biological transmission Effects 0.000 claims description 2
- 239000000463 material Substances 0.000 claims description 2
- 238000011084 recovery Methods 0.000 abstract description 9
- 238000002485 combustion reaction Methods 0.000 description 10
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 239000000203 mixture Substances 0.000 description 4
- 239000002699 waste material Substances 0.000 description 4
- 230000005611 electricity Effects 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 2
- 238000002309 gasification Methods 0.000 description 2
- 230000004048 modification Effects 0.000 description 2
- 238000012986 modification Methods 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 239000000779 smoke Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 230000006641 stabilisation Effects 0.000 description 1
- 238000011105 stabilization Methods 0.000 description 1
Images
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
- F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
- F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
- F17C7/02—Discharging liquefied gases
- F17C7/04—Discharging liquefied gases with change of state, e.g. vaporisation
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- 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
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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
- 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
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- 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
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- 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
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- 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
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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
- 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
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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
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/03—Treating the boil-off
- F17C2265/032—Treating the boil-off by recovery
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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
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/06—Fluid distribution
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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
- F17C2265/00—Effects achieved by gas storage or gas handling
- F17C2265/07—Generating electrical power as side effect
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- 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]
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- 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
Abstract
The invention discloses a BOG and LNG cold energy comprehensive recycling system and a process, wherein the system 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, an LNG immersed pump, an LNG booster pump, a BOG buffer tank, a condensation regasification system BOG compressor, a pressurization LNG-BOG pre-cooler and a BOG re-condenser; the BOG direct compression output system comprises a BOG seawater preheater, an output system BOG compressor and a BOG seawater cooler; the BOG cogeneration system comprises a cogeneration 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 BOG recovery system is suitable for BOG recovery systems under different working conditions, and the problem that the BOG production fluctuation is too large and the recovery is difficult is solved.
Description
Technical Field
The invention belongs to the field of comprehensive energy recovery and utilization of LNG (liquefied natural gas) receiving stations, and particularly relates to a BOG and LNG cold energy comprehensive recovery and utilization system and process.
Background
As last half year of 2019, domestic built and put into production LNG stations reach 21 seats, but cold energy generated in the LNG receiving and unloading process is not well utilized. Meanwhile, a large amount of BOG (LNG vaporized gas) is generated in the operation process of the LNG receiving station, and the LNG receiving station cannot be well recycled, only a small amount of BOG (flash gas) is recycled at present, and most of BOG is combusted and discharged through a torch system, so that energy waste is caused. The two parts cause a great deal of energy waste, and further cause great economic loss. Therefore, the design of a proper LNG cold energy utilization and BOG recycling method has important significance.
The Chinese patent document with the publication number of CN109386316A and the name of a combined utilization system and method of LNG cold energy and BOG combustion energy discloses a combined utilization system of LNG cold energy and BOG combustion energy, wherein high-temperature steam generated by BOG combustion is used for generating 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 is used for providing heat energy for a heat supply subsystem, so that the purpose of improving the power generation efficiency of the system is achieved. However, the technology is limited by the load range of the BOG gas turbine, has low flexibility, and cannot well process the BOG gas turbine when the BOG load fluctuation of the LNG receiving station is large.
Chinese patent document CN109404079A entitled BOG recondensing and LNG cold power generation integrated system for LNG receiving station discloses a method for using LNG cold power generation for BOG recondensing process. However, the efficiency of converting the cold energy of the low-temperature Rankine cycle into the electric energy is low, so the utilization efficiency of the method is not high.
Therefore, a process with high energy recovery rate and high operational flexibility, which can well cope with the BOG load fluctuation of the LNG receiving station, is required to recover the cold energy of the LNG receiving station and the generated BOG. The process takes a peak-adjusting LNG receiving station as an example, LNG cold energy utilization and BOG recycling are skillfully combined, BOG production fluctuation in different periods is considered to be large, BOG is cooperatively recovered by adopting condensation regasification, combustion power generation and direct compression processes, and hot water generated by flue gas waste heat after BOG combustion power generation is used for providing a heat source for LNG cold energy power generation, so that the process has strong cooperativity and good operation elasticity, and the waste of BOG is reduced while LNG cold energy power generation is fully realized.
Disclosure of Invention
The invention aims to provide a BOG and LNG cold energy recycling process suitable for an LNG receiving station, aiming at the problem that the BOG and LNG cold energy generated in the operation process of the existing LNG receiving station is not well recycled, so that the complementary energy of the LNG receiving station can be cooperatively recycled, and the energy utilization rate of the LNG receiving station is improved. According to the difference of LNG external output and BOG output in the LNG receiving station base load non-unloading period, the LNG unloading period, the peak regulation non-unloading period and the peak regulation unloading period, condensation regasification, combustion power generation and direct compression processes are respectively arranged to cooperatively recover the BOG, and meanwhile, hot water generated by waste heat of flue gas generated after the BOG combustion power generation is used for providing 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 by at least 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 pressure pump, a BOG buffer tank, a condensation regasification system BOG compressor, a pressurization LNG-BOG pre-cooler and a BOG re-condenser, wherein the pressurization LNG-BOG pre-cooler and the BOG re-condenser are connected with the LNG pressure pump; the LNG storage tank, the BOG buffer tank, the BOG compressor of the condensation regasification system, the pressurization LNG-BOG precooler and the BOG recondenser are sequentially connected; the LNG immersed pump divides natural gas in the LNG storage tank into two parts, and the LNG booster pump and the BOG recondenser are both connected with the LNG immersed pump; the LNG pressurization pump divides the pressurized LNG into two streams, one stream is sent to a pressurization LNG-BOG precooler to precool the BOG from the BOG buffer tank, and the other stream is mixed with the precooled LNG and then sent to a downstream external transportation and LNG cold energy power generation system;
the BOG direct compression output system comprises a BOG seawater preheater, a BOG direct compression output system BOG compressor and a BOG seawater cooler, wherein the BOG seawater preheater, the BOG direct compression 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 sequentially connected;
the BOG cogeneration system comprises a thermoelectric system BOG compressor connected with the BOG seawater preheater, 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 connected with the BOG pressure regulating and metering equipment; the BOG compressor of the thermoelectric system, the BOG pressure regulating and metering device, the first gas turbine generator set and the flue gas waste heat boiler are sequentially connected;
the LNG cold energy power generation system comprises an LNG raw seawater vaporizer, a natural gas metering system connected with the LNG raw seawater vaporizer, 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 sparse way.
According to the BOG condensation regasification system, LNG at the temperature of minus 164 to minus 161 ℃ in an LNG storage tank and at the pressure of 1.15bar is pressurized to 4-6 bar by an LNG immersed pump and then divided into two parts, one part is conveyed to an LNG pressure pump, and the other part enters a BOG recondenser to condense the BOG;
the LNG pressurized by the LNG pressurization pump is divided into two streams, one stream is sent to a pressurization 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;
after BOG which is led out from the LNG storage tank and has the temperature of-150 ℃ and the pressure of 1.15bar enters a BOG buffer tank, leading out the BOG from a BOG buffer tank, compressing the BOG to 4-6 bar by a BOG compressor of a condensation regasification system, wherein the pressure is consistent with the LNG pressure at the outlet of the LNG immersed pump, precooling and heat exchanging the compressed BOG and part of LNG pressurized by an LNG pressure pump in a pressurization LNG-BOG precooler, cooling to-100 to-90 ℃, then the mixture enters a BOG recondensor to directly contact with one LNG coming out of an LNG immersed pump for heat exchange and condensation, the temperature is reduced to minus 135 to minus 142 ℃, the mixture is mixed with the other LNG coming out of the LNG immersed pump after coming out of the BOG recondensor, the temperature is reduced to minus 138 to minus 145 ℃, the mixture enters a booster pump for pressurization to 65bar, the temperature is increased to minus 135 to minus 142 ℃, one part of pressurized LNG precools BOG again, and the other part of pressurized LNG enters the downstream after being mixed with the precooled LNG after heat exchange;
the BOG direct compression output system comprises a BOG buffer tank, a BOG seawater preheater, a BOG compressor, a BOG direct compression output system and a BOG seawater cooler, wherein BOG which is led out from an LNG storage tank and is at-150 ℃ and 1.15bar enters the BOG buffer tank, is preheated to-55 to-50 ℃ through the BOG seawater preheater, then enters the BOG direct compression output system and is compressed to 4bar through the BOG compressor, and then is cooled through the BOG seawater cooler and output to a medium-low pressure pipe network;
the BOG cogeneration system is characterized in that BOG which is led out from an LNG storage tank at-150 ℃ and 1.15bar enters a BOG buffer tank, then flows through a BOG seawater preheater to be preheated to-55 to-50 ℃, is compressed to 16 to 20bar by a BOG compressor of the cogeneration system, and enters a first gas turbine generator set and a second gas turbine generator set to generate electricity after passing through a pressure regulating metering device; introducing the flue gas into a flue gas waste heat boiler, exchanging heat with cold water at the temperature of 25-35 ℃, and using the generated hot water at the temperature of 65-75 ℃ as a circulating heat source of the LNG cold energy power generation system;
in the LNG cold energy power generation system, 65bar LNG at-132 to-140 ℃ from the LNG booster pump is divided into two paths, one path of LNG is gasified along an LNG original seawater gasifier and then is transmitted outwards, the other path of LNG exchanges heat with a mixed working medium through an LNG-mixed working medium heat exchanger, and natural gas after heat exchange is heated to 0 ℃ through an LNG seawater reheater and then is sent to an external transmission pipe network through a natural gas metering system;
the mixed working medium is cooled to be in a liquid state through the LNG-mixed working medium heat exchanger, the mixed working medium enters the mixed working medium storage tank, the liquid mixed working medium discharged from the mixed working medium storage tank is pressurized through the mixed working medium booster pump, then the mixed working medium enters the mixed working medium reheater and is heated to be in a gaseous state by circulating hot water generated in the flue gas waste heat boiler, the mixed working medium enters the expansion generator to generate power, an outlet of the expansion generator is connected with a hot material inflow port of the LNG-mixed working medium heat exchanger, the expanded low-temperature and low-pressure gaseous mixed working medium enters the LNG-mixed working medium heat exchanger to exchange.
Furthermore, the mixed working medium of the LNG cold energy power generation system is a combination of at least two of the organic working media.
Furthermore, a 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.
And furthermore, a feedback regulating valve is arranged at the LNG shunting position in front of the LNG-mixed working medium heat exchanger, the LNG-mixed working medium heat exchanger is regulated according to the fluctuation of the use amount of downstream natural gas, and when the demand of the natural gas is too large or too small, the LNG raw seawater vaporizer is opened to vaporize, and then the LNG-mixed working medium heat exchanger is conveyed to downstream after pressure regulation and metering.
Further, the process fully considers the fluctuation change of the BOG along with the LNG and whether the BOG is unloaded, and aiming at four different conditions mainly existing in the LNG receiving station, namely a base load non-unloading period, a base load unloading period, a peak regulation non-unloading period and a peak regulation unloading period, the BOG generated by the BOG condensation regasification system, the BOG direct compression output system and the BOG cogeneration system is utilized.
Further, in the period of basic load output and non-unloading, the BOG production is minimum, at the moment, a gas turbine is started to carry out recovery combustion on the BOG, and condensation, regasification and compression are not adopted to enter a medium-low pressure pipe network facility.
Further, during the period of basic load export and ship unloading, the LNG export amount is unchanged, the BOG generation amount is increased due to the ship unloading reason, the export LNG is liquefied by a BOG condensation regasification system, two gas turbines are started to recover the BOG, and the rest BOG is treated by a compression and retraction pipe network.
Further, in the peak-shaving external transportation and non-ship unloading period, the LNG external transportation amount is increased rapidly, the BOG generation amount is further increased, the BOG treatment amount of the BOG condensation regasification system is also increased along with the increase of the LNG external transportation amount, at the moment, two gas turbines are started to recover, burn, generate power, condense and regasify the BOG, and the rest BOG enters a medium-low pressure pipe network after being compressed.
Further, during peak load regulation export and ship unloading periods, the LNG export amount is increased rapidly, the BOG production amount is the maximum, at the moment, the BOG condensation regasification system, the BOG direct compression export system and the BOG combined heat and power generation system are started at full load, and the rest BOG is combusted through a flare.
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 inlet network system are used for recycling the BOG, so that the process has strong cooperativity and good operation elasticity.
2. The waste heat of the flue gas after BOG combustion power generation is utilized to generate hot water for providing a heat source for LNG cold energy power generation, and the waste of BOG is reduced while the LNG cold energy power generation is fully realized.
3. The problem of the too big recovery difficulty of BOG production fluctuation is solved, LNG cold energy generating efficiency and the energy utilization of receiving station have been improved.
Drawings
FIG. 1 is a schematic diagram of a BOG and LNG cold energy comprehensive recycling process according to an embodiment of the present invention;
the figures show that: 1-LNG storage tank, 2-LNG immersed pump, 3-LNG booster pump, 4-LNG raw seawater vaporizer, 5-natural gas metering system, 6-BOG buffer tank, 7-condensation regasification system BOG compressor, 8-pressure LNG-BOG precooler, 9-BOG recondenser, 10-BOG seawater preheater, 11-BOG direct compression export system BOG compressor, 12-BOG seawater cooler, 13-LNG-mixed working medium heat exchanger, 14-LNG seawater reheater, 15-mixed working medium storage tank, 16-mixed working medium booster pump, 17-mixed working medium reheater, 18-expansion generator, 19-thermoelectric system BOG compressor, 20-BOG pressure regulating metering equipment, 21-flue gas waste heat boiler, 22-first gas turbine generator set, 23-second gas turbine genset.
Detailed Description
For a better understanding of the present invention, reference is made to the following examples and accompanying drawings, but the scope of the invention as claimed is not limited to the examples.
Certain peak regulation type LNG receiving station construction scale 500 × 104t/a, the LNG external basic load is kept at 150 x 104Sm3D (45 t/h), and the peak-shaving output is 1800 x 104Sm3And d (585 t/h), the temperature of the LNG discharged from the storage tank is-161 ℃, and the gasification pressure is 8 MPa. Maximum gasification output capacity of 6000 x 104Sm3/d。
The BOG output of the LNG receiving station during the external transportation without unloading the base load is 6.12-6.36 t/h, the BOG output of the LNG receiving station during the external transportation without unloading the base load is 22.94-23.10 t/h, the BOG output of the LNG receiving station during the external transportation without unloading the peak regulation is 43.81-44.68 t/h, and the BOG output of the LNG receiving station during the external transportation without unloading the base load is 60.39-63.46 t/h. The station is provided with a BOG condensation regasification system, the treatment capacity is 20t/h, and two BOG compressors with 9000 sides (the total treatment capacity is 12.16 t/h) can compress BOG into a 0.4MPa pipe network. In addition, the BOG recovery system is adjusted by adding two sets of gas turbine power generation sets with the design scale of 6 t/h.
The comprehensive BOG and LNG cold energy recycling system shown in FIG. 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 and 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 and regasification system BOG compressor 7, a pressurization LNG-BOG pre-cooler 8 and a BOG re-condenser 9, wherein the pressurization LNG-BOG pre-cooler 8 and the BOG re-condenser 9 are 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 pressurization 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 both connected with the LNG immersed pump 2; the LNG pressurization pump 3 divides the pressurized LNG into two streams, one stream is sent to a pressurization LNG-BOG precooler 8 to precool the BOG from the BOG buffer tank 6, and the other stream is mixed with the precooled LNG and then sent to a downstream external transportation and LNG cold energy power generation system;
the BOG direct compression output system comprises a BOG seawater preheater 10, a BOG direct compression output system BOG compressor 11 and a BOG seawater cooler 12 which are connected with the BOG buffer tank 6; the BOG seawater preheater 10, the BOG direct compression output system BOG compressor 11 and the BOG seawater cooler 12 are sequentially connected;
the BOG cogeneration system comprises a thermoelectric system BOG compressor 19 connected with the 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 and metering device 20, the first gas turbine generator set 22 and the flue gas waste heat boiler 21 of the thermoelectric system are sequentially connected;
the LNG cold energy power generation system comprises an LNG raw seawater vaporizer 4, a natural gas metering system 5 connected with the LNG raw seawater vaporizer 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 connected in sequence.
The technological process of the BOG and LNG cold energy comprehensive recycling system is as follows:
BOG condensation regasification system: LNG at the temperature of-161 ℃ and 1.15bar in an LNG storage tank 1 is pressurized to 5.5bar by an LNG immersed pump 2, the LNG is divided into two parts, one part is conveyed to an LNG pressurizing pump 3, and the other part enters a BOG recondenser 9 to condense BOG;
the LNG pressurized by the LNG pressurizing pump 3 is divided into two streams, one stream is sent to a pressurizing 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 transportation and LNG cold energy power generation system;
BOG at-150 ℃ and 1.15bar is led out from the top of an LNG storage tank 1, enters a BOG buffer tank 6 for pressure stabilization, is compressed to 5.5bar by a BOG compressor 7 of a condensation regasification system, is cooled to-100 ℃ and then enters a BOG recondenser 9 to be directly contacted with one LNG stream coming out of an LNG immersed pump 2 for heat exchange and condensation after being heated to-67.49 ℃, is mixed with the other LNG stream coming out of the LNG immersed pump 2 after being discharged from the BOG recondenser 9, is cooled to-139.19 ℃, enters a pressurization pump 3 for pressurization to 65bar, and is heated to-134.76 ℃. And a part of pressurized LNG precools BOG again, and the mixed temperature of the other part of LNG and precooled heat-exchanged LNG at-131.78 ℃ is increased to-132.38 ℃ and then enters the downstream. The process can liquefy 1t of BOG per 6.86t of LNG.
BOG direct compression export system: BOG which is led out from an LNG storage tank 1 and has the temperature of-150 ℃ and the pressure of 1.15bar enters a BOG buffer tank 6, is preheated to-55 to-50 ℃ by a BOG seawater preheater 10, then enters a BOG compressor 11 of a BOG direct compression output system to be compressed to 4bar, is cooled by a BOG seawater heat exchanger 12 and then is output to a medium-low pressure pipeline.
The BOG cogeneration system: BOG of-150 ℃ and 1.15bar is led out from an LNG storage tank 1, enters a BOG buffer tank 6, flows through a BOG seawater preheater 10 to be preheated to-55 ℃, is compressed to 18bar through a BOG compressor 19 of a thermoelectric system, enters a first gas turbine generator set 22 and a second gas turbine generator set 23 through a pressure regulating metering device 20 to generate electricity, tail gas is led into a flue gas waste heat boiler 21 to exchange heat with cold water of 30 ℃, and the generated hot water of 70 ℃ is used as a circulating heat source of an LNG cold energy power generation system.
LNG cold energy power generation system: the 65bar LNG coming out of the BOG condensation regasification system is divided into two paths at the temperature of-132.38 ℃, one path of LNG is output outwards along the original LNG original seawater vaporizer 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 (mixed ethane and propane). The natural gas after heat exchange is heated to 0 ℃ by an LNG seawater reheater 14, passes through an original natural gas metering system 5 of an LNG receiving station and passes through a natural gas output main pipe and an external conveying pipe network;
the liquid C2C3 with the pressure of 0.2MPa and the temperature of-61 ℃ coming out from a mixed working medium refrigerant storage tank 15 (in the embodiment, the mixed working medium is C2C3, namely the mixture of ethane and propane) is pressurized to 1.1MPa by a mixed working medium booster pump 16, the temperature is increased to-60 ℃, then the liquid C2C3 passes through a mixed working medium reheater 17, is heated to 40 ℃ (gaseous state) by hot water with the temperature of 70 ℃ and normal pressure generated in a flue gas waste heat boiler 21, enters an expansion generator 18 for expansion power generation, is expanded to 0.2MPa, the temperature is reduced to-19 ℃, enters an LNG-mixed working medium heat exchanger 13 for heat exchange, and the temperature is reduced to. The LNG cold energy power generation system can generate about 20kW for 1t of LNG, 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 period of basic load output and non-unloading, the LNG output is 45t/h, the BOG output 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 for entering a medium-low pressure pipe network.
During the period of base load export and ship unloading, the LNG export amount is 45t/h, the BOG generation amount is about 23t/h, 6.56t/h of BOG can be treated by condensation and regasification, two gas turbines are started to burn at the moment to recover the BOG (12 t/h), and the residual 4.44t/h of BOG is treated by compressing and retracting a pipe network.
During the peak load-shifting period and the non-unloading period, the LNG load-shifting amount is increased to 585t/h, the BOG production amount is about 44t/h, and 20t/h of BOG can be treated by condensation and regasification. At the moment, two gas turbines can be started to recover and burn the BOG for power generation and start a BOG condensation and regasification system, and the remaining 12t/h of BOG is compressed and enters a medium-low pressure pipe network.
During peak-shaving export and ship unloading periods, the LNG export amount is increased to 585t/h, the BOG production amount is 60.39-63.46 t/h, at the moment, two gas turbines can be started at full load to recover, burn and generate power for BOG, a BOG condensation regasification system, a BOG direct compression export system and a BOG cogeneration system are started, hot water is generated by residual BOG combusted smoke through the smoke waste heat boiler 21 and is used for reheating mixed working media in the LNG cold energy power generation process, and the LNG cold energy power generation efficiency is improved by about 25%.
The above examples of the present invention are merely examples for clearly illustrating the present invention and are not intended to limit the embodiments of the present invention. Other variations and modifications will be apparent to persons skilled in the art in light of the above description. And are neither required nor exhaustive of all embodiments. Any modification, equivalent replacement, and improvement made within the spirit and principle of the present invention should be included in the protection scope of the claims of the present invention.
Claims (10)
1. The utility model provides a BOG and LNG cold energy comprehensive recycling system which characterized in that: the system 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 and regasification system comprises an LNG storage tank (1), an LNG immersed pump (2), an LNG pressure pump (3), a BOG buffer tank (6), a condensation and regasification system BOG compressor (7), a pressurization LNG-BOG pre-cooler (8) and a BOG re-condenser (9), wherein the pressurization LNG-BOG pre-cooler is connected with the LNG pressure pump (3); the LNG storage tank (1), the BOG buffer tank (6), the BOG compressor (7) of the condensation regasification system, the pressurization LNG-BOG pre-cooler (8) and the BOG re-condenser (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 both connected with the LNG immersed pump (2); the LNG pressurized by the LNG pressurizing pump (3) is divided into two streams, one stream is sent to a pressurized LNG-BOG precooler (8) to precool BOG from the BOG buffer tank (6), and the other stream is mixed with the precooled LNG and then sent to a downstream external transportation and LNG cold energy power generation system;
the BOG direct compression output system comprises a BOG seawater preheater (10) connected with the BOG buffer tank (6), a BOG direct compression output system BOG compressor (11) 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 sequentially connected;
the BOG cogeneration system comprises a BOG compressor (19) of the thermoelectric system, 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), wherein the BOG compressor (19) of the thermoelectric system is connected with the BOG seawater preheater (10); the BOG compressor (19), the BOG pressure regulating and metering device (20), the first gas turbine generator set (22) and the flue gas waste heat boiler (21) of the thermoelectric system are sequentially connected;
the LNG cold energy power generation system comprises an LNG original seawater vaporizer (4), a natural gas metering system (5) connected with the LNG original seawater vaporizer (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 connected in a diluted mode.
2. The utilization process of the BOG and LNG cold energy comprehensive recycling system according to claim 1, characterized in that: in the BOG condensation and regasification system, LNG at the temperature of minus 164 to minus 161 ℃ and 1.15bar in an LNG storage tank (1) is pressurized to 4-6 bar by an LNG immersed pump (2) and then divided into two parts, one part is conveyed to an LNG pressure pump (3), and the other part enters a BOG recondenser (9) to condense BOG;
the LNG pressurized by the LNG pressurizing pump (3) is divided into two streams, one stream is sent to a pressurizing LNG-BOG precooler (8) to precool the BOG from the BOG buffer tank (6), and the other stream is mixed with the LNG fed back after precooling and then sent to a downstream external transportation and LNG cold energy power generation system;
leading BOG (boil-off gas) which is led out from an LNG (liquefied natural gas) storage tank (1) at-150 ℃ and 1.15bar into a BOG buffer tank, leading out from a BOG buffer tank (6), compressing the BOG into 4-6 bar by a BOG compressor (7) of a condensation regasification system, wherein the pressure is consistent with the LNG pressure at an outlet of an LNG immersed pump (3), precooling and exchanging heat between the compressed BOG and partial LNG pressurized by an LNG pressurizing pump (3) in a pressurization LNG-BOG precooler (8), cooling to-100 to-90 ℃, then entering a BOG recondenser (9) to directly contact with one LNG coming out of the LNG immersed pump (2) for heat exchange and condensing, cooling to-135-142 ℃, mixing the BOG going out of the BOG recondenser (9) with the other coming out of the LNG immersed pump (2), cooling to-138 to-145 ℃, entering the pressurizing pump (3) to 65, increasing the temperature to-135 to-142 ℃, precooling BOG again by one part of pressurized LNG, and mixing the other part of pressurized LNG with the precooled heat-exchanged LNG and then entering the downstream;
the BOG direct compression output system comprises a BOG buffer tank (6), a BOG seawater preheater (10) for preheating BOG at-150 ℃ and 1.15bar, a BOG compressor (11) of the BOG direct compression output system for compressing to 4bar, a BOG seawater cooler (12) for cooling and outputting to a medium-low pressure pipe network, wherein BOG is led out from an LNG storage tank (1) and enters the BOG buffer tank (6);
the BOG cogeneration system is characterized in that BOG which is led out from an LNG storage tank (1) and is at-150 ℃ and 1.15bar enters a BOG buffer tank (6), then flows through a BOG seawater preheater (10) to be preheated to-55 to-50 ℃, is compressed to 16 to 20bar through a BOG compressor (19) of a thermoelectric system, and then enters a first gas turbine generator set (22) and a second gas turbine generator set (23) to generate power after passing through a pressure regulating metering device (20); introducing the flue gas into a flue gas waste heat boiler (21), exchanging heat with cold water at the temperature of 25-35 ℃, and using the generated hot water at the temperature of 65-75 ℃ as a circulating heat source of the LNG cold energy power generation system;
in the LNG cold energy power generation system, 65bar LNG at-132 to-140 ℃ from the LNG booster pump (3) is divided into two paths, one path of LNG is gasified along the LNG original seawater gasifier (4) and then transmitted outwards, the other path of LNG exchanges heat with a mixed working medium through the LNG-mixed working medium heat exchanger (13), and natural gas after heat exchange is heated to 0 ℃ through the LNG seawater reheater (14) and then is sent to an external transmission pipe network through the natural gas metering system (5);
the mixed working medium is cooled to be in a liquid state through the LNG-mixed working medium heat exchanger (13), the mixed working medium enters the mixed working medium storage tank (15), the liquid mixed working medium discharged from the mixed working medium storage tank (15) is pressurized through the mixed working medium booster pump (16), then the mixed working medium enters the mixed working medium reheater (17) and is heated to be in a gas state through circulating hot water generated in the flue gas waste heat boiler (21), the mixed working medium enters the expansion generator (18) for power generation, an outlet of the expansion generator (18) is connected with a hot material inflow port of the LNG-mixed working medium heat exchanger (13), the expanded low-temperature and low-pressure gas mixed working medium enters the LNG-mixed working medium heat exchanger (13) to exchange heat and condense with.
3. The BOG and LNG cold energy comprehensive recycling process of claim 2, characterized in that: the mixed working medium of the LNG cold energy power generation system is a combination of at least two of the organic working media.
4. The BOG and LNG cold energy comprehensive recycling process of claim 2, characterized in that: 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).
5. The BOG and LNG cold energy comprehensive recycling process of claim 2, characterized in that: the LNG-mixed working medium heat exchanger (13) is provided with a feedback regulating valve at the front LNG shunting position, the LNG-mixed working medium heat exchanger is regulated according to the fluctuation of the use amount of downstream natural gas, when the demand amount of the natural gas is too large or too small, the LNG raw seawater vaporizer (4) is opened to be vaporized, and then the LNG raw seawater vaporizer is conveyed to the downstream after being measured by pressure regulation (5).
6. The BOG and LNG cold energy comprehensive recycling process of claim 2, characterized in that: aiming at four different conditions mainly existing in the LNG receiving station, namely a base load non-ship unloading period, a base load ship unloading period, a peak regulation non-ship unloading period and a peak regulation ship unloading period, the BOG generated by the BOG condensation regasification system, the BOG direct compression export system and the BOG cogeneration system is utilized.
7. The BOG and LNG cold energy comprehensive recycling process of claim 6, characterized in that: when the basic load is transported out and is not unloaded, the BOG production amount is minimum, at the moment, a gas turbine is started to recover and burn the BOG, and condensation, regasification and compression are not adopted to enter a medium-low pressure pipe network.
8. The BOG and LNG cold energy comprehensive recycling process of claim 6, characterized in that: during the period of basic load export and ship unloading, the LNG export volume is unchanged, the BOG production volume is increased due to the ship unloading reason, the export LNG is liquefied by a BOG condensation regasification system, two gas turbines are started to recover the BOG, and the rest BOG is treated by a compression and retraction pipe network.
9. The BOG and LNG cold energy comprehensive recycling process of claim 6, characterized in that: during peak-shaving export and non-ship-unloading periods, the LNG export volume is increased rapidly, the BOG production volume is further increased, the BOG treatment volume of the BOG condensation and regasification system is also increased along with the increase of the LNG export volume, at the moment, two gas turbines are started to recover, burn, generate power, condense and regasify the BOG, and the residual BOG is compressed and enters a medium-low pressure pipe network.
10. The BOG and LNG cold energy comprehensive recycling process of claim 6, characterized in that: during peak-shaving export and ship unloading periods, the LNG export amount is increased sharply, the BOG production amount is the maximum, at the moment, the BOG condensation regasification system, the BOG direct compression export system and the BOG cogeneration system are started at full load, and the rest BOG is combusted through a torch.
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