CN107166871A - Using the re-liquefied system of natural gas vaporization gas of twin-stage mixed-refrigerant cycle - Google Patents
Using the re-liquefied system of natural gas vaporization gas of twin-stage mixed-refrigerant cycle Download PDFInfo
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- 239000003507 refrigerant Substances 0.000 title claims abstract description 102
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 53
- 239000007789 gas Substances 0.000 title claims abstract description 21
- 239000003345 natural gas Substances 0.000 title claims abstract description 19
- 238000009834 vaporization Methods 0.000 title claims abstract description 12
- 230000008016 vaporization Effects 0.000 title claims abstract description 12
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 230000004087 circulation Effects 0.000 claims abstract description 14
- 238000005057 refrigeration Methods 0.000 claims abstract description 12
- 230000006835 compression Effects 0.000 claims abstract description 9
- 238000007906 compression Methods 0.000 claims abstract description 9
- 239000000203 mixture Substances 0.000 claims description 30
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 claims description 16
- 239000012530 fluid Substances 0.000 claims description 12
- NNPPMTNAJDCUHE-UHFFFAOYSA-N isobutane Chemical compound CC(C)C NNPPMTNAJDCUHE-UHFFFAOYSA-N 0.000 claims description 8
- 239000001294 propane Substances 0.000 claims description 8
- 238000009833 condensation Methods 0.000 claims description 7
- 230000005494 condensation Effects 0.000 claims description 7
- 239000007791 liquid phase Substances 0.000 claims description 5
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 claims description 4
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 claims description 4
- 239000003795 chemical substances by application Substances 0.000 claims description 4
- 239000001282 iso-butane Substances 0.000 claims description 4
- 235000013847 iso-butane Nutrition 0.000 claims description 4
- 239000007792 gaseous phase Substances 0.000 claims description 3
- 239000007921 spray Substances 0.000 claims 1
- 238000000034 method Methods 0.000 abstract description 10
- 230000000694 effects Effects 0.000 abstract description 2
- 230000002427 irreversible effect Effects 0.000 abstract description 2
- 230000002265 prevention Effects 0.000 abstract description 2
- 239000003949 liquefied natural gas Substances 0.000 description 16
- 238000001816 cooling Methods 0.000 description 8
- 239000012071 phase Substances 0.000 description 7
- 238000005096 rolling process Methods 0.000 description 5
- 238000002309 gasification Methods 0.000 description 3
- 230000009102 absorption Effects 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000004781 supercooling Methods 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000005431 greenhouse gas Substances 0.000 description 1
- 239000012263 liquid product Substances 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010025 steaming Methods 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
Classifications
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0219—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle in combination with an internal quasi-closed refrigeration loop, e.g. using a deep flash recycle loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
- F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/0052—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by vaporising a liquid refrigerant stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0257—Construction and layout of liquefaction equipments, e.g. valves, machines
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2240/00—Processes or apparatus involving steps for expanding of process streams
- F25J2240/60—Expansion by ejector or injector, e.g. "Gasstrahlpumpe", "venturi mixing", "jet pumps"
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
Using the re-liquefied system of natural gas vaporization gas of twin-stage mixed-refrigerant cycle, including high-temperature region mix refrigerant (MR2) circulation, low-temperature space mix refrigerant (MR1) circulation and BOG ejector refrigeration liquefaction cycles, using the twin-stage mixed refrigerant systems with injector, two-stage mix refrigerant kind of refrigeration cycle is set by rational component proportion, pressure and temperature, makes the BOG after compression re-liquefied with less wasted work amount；Injector is introduced simultaneously, using the BOG in high-pressure liquid prevention of natural gas ejected storage tank, the irreversible loss in throttling process is reduced, saves wasted work, the unit liquefaction wasted work amount of system is reduce further, and energy-saving effect is notable.
Description
Technical field
The invention belongs to LNG Technology field, and in particular to natural using the liquefaction of twin-stage mixed-refrigerant cycle
The re-liquefied system of gas boil-off gas.
Background technology
Liquefied natural gas (liquefied natural gas, LNG) is the cryogenic liquid that a kind of normal pressure is stored in -162 DEG C
Fuel, its main component is methane, 1/625 when volume is gaseous state, it is easy to transport for long-distance and stores.Because LNG normal pressure is store
Temperature is deposited for -162 DEG C, its transport and storage process in, there is heat to be leak into from environment unavoidably, part LNG vaporization is produced steaming
Got angry (boil-off gas, BOG), and raises container pressure, and when pressure is higher than safe pressure, BOG will be disposed to greatly
In gas, greenhouse gas emission is not only caused, economic loss is also very considerable, therefore how rationally to reclaim BOG as LNG storage ring
Section hot issue urgently to be resolved hurrily.
At present, BOG handling process is generally recondensation process, defeated, the LNG being subcooled using high pressure outside technique combination LNG
The BOG after compression is condensed, vaporizer is pumped to again afterwards, LNG cold has been reclaimed, the wasted work of BOG pressurizations is greatlyd save.
However, when outside LNG storage tank defeated load it is smaller or for a long time without it is defeated outside LNG when, the BOG constantly produced will be emptied by torch, with tie up
Hold the safe pressure of system operation.Therefore, the technique fundamentally can not effectively solve BOG process problem, need to consider to adopt
With independent cryogenic refrigerating system by BOG it is re-liquefied after send back in storage tank.
The content of the invention
In order to overcome the shortcoming of above-mentioned prior art, object of the present invention is to provide followed using twin-stage mix refrigerant
The re-liquefied system of natural gas vaporization gas of ring, makes its unit liquid product energy consumption lower, can effectively reduce BOG re-liquefied
Wasted work.
To achieve these goals, the present invention is adopted the following technical scheme that：
Using the re-liquefied system of natural gas vaporization gas of twin-stage mixed-refrigerant cycle, including heat exchanger HX1, heat exchange
Device HX1 outlet c is connected with first order high temperature refrigerant compressor C6 entrances, the first order high temperature refrigerant compressor C6 outlet and
The entrance of 5th cooler 5 is connected, the outlet of the 5th cooler 5 and the connection of second level high temperature refrigerant compressor C7 entrances, the second level
High temperature refrigerant compressor C7 outlets are connected with the entrance of the 6th cooler 6, the outlet of the 6th cooler 6 and heat exchanger HX1 entrance e
Connection, and the heat exchanger HX1 of entrance e connections outlet f are connected with high temperature refrigerant choke valve V2 entrances, high temperature refrigerant throttling
Valve V2 outlets are connected with heat exchanger HX1 entrance d, and entrance d is connected with outlet c, are constituted high-temperature region mix refrigerant (MR2) and are followed
Ring；
Heat exchanger HX1 outlet a is connected with first order low-temperature refrigerant compressor C4 entrances, first order low-temperature refrigerant pressure
Contracting machine C4 outlets are connected with the entrance of the 3rd cooler 3, the outlet of the 3rd cooler 3 and second level low-temperature refrigerant compressor C5 entrances
Connection, second level low-temperature refrigerant compressor C5 outlets and the connection of the entrance of the 4th cooler 4, the outlet of the 4th cooler 4 and heat exchange
Device HX1 entrance g connections, and the heat exchanger HX1 of entrance g connections outlet h are connected with heat exchanger HX2 entrance m, and entrance m
The heat exchanger HX2 of connection outlet n is connected with low-temperature refrigerant choke valve V1 entrances, and low-temperature refrigerant choke valve V1 is exported with changing
Hot device HX2 entrance l connections, and the heat exchanger HX2 of entrance l connections outlet k are connected with heat exchanger HX1 entrance b, entrance b
Connected with heat exchanger HX1 outlet a, constitute low-temperature space mix refrigerant (MR1) circulation；
Heat exchanger HX1 outlet j is connected with heat exchanger HX2 entrance o, the heat exchanger HX2 connected with entrance o outlet p
It is connected with subcooler HX3 entrance s, the subcooler HX3 connected with entrance s outlet t and injector E0 main fluid entrances u connect
Connect, injector E0 driven fluid entrance v and storage tank BOG outlet is connected, and injector E0 outlet w and gas-liquid separator S0 enter
Mouth x connections, gas-liquid separator S0 liquid-phase outlet y and BOG choke valve V0 entrances are connected, BOG choke valves V0 outlets and LNG storage tank
Connection；The gaseous phase outlet z and subcooler HX3 of gas-liquid separator entrance r connections, the subcooler HX3 connected with entrance r outlet
Q is connected with first order BOG compressor C1 entrances, and first order BOG compressors C1 exports the entrance phase with second level BOG compressors C2
Even, second level BOG compressors C2 outlet and the entrance of the first cooler 1 are connected, the outlet of the first cooler 1 and the third level
BOG compressor C3 entrances are connected, and third level BOG compressors C3 outlets are connected with the entrance of the second cooler 2, and the second cooler 2 goes out
Mouth is connected with heat exchanger HX1 entrance i, and entrance i is connected with heat exchanger HX1 outlet j, so far constitutes the liquefaction of BOG ejector refrigerations
Circulation.
Described high-temperature region mix refrigerant includes iso-butane, propane and ethane, and the low-temperature space mix refrigerant is included
Propane, ethene and methane.
Described high-temperature region mix refrigerant (MR2), which is recycled into before heat exchanger HX1, realizes all condensation, described low temperature
Area's mix refrigerant (MR1) realizes partial condensation before being recycled into heat exchanger HX2.
Described BOG ejector refrigerations liquefaction cycle realizes all liquefaction before subcooler HX3 is entered.
Beneficial effects of the present invention are：
The present invention is used for the re-liquefied recyclings of BOG in storage tank, using a kind of twin-stage hybrid refrigeration with injector
Agent system, the advantage is that two-stage mix refrigerant kind of refrigeration cycle by rational component proportion, pressure and temperature set, with compared with
Small wasted work amount makes the BOG after compression re-liquefied.Meanwhile, the system introduces injector, is stored up using high-pressure liquid prevention of natural gas ejected
BOG in tank, reduces the irreversible loss in throttling process, saves wasted work, reduce further the unit liquefaction of system
Wasted work amount, energy-saving effect is notable.
Brief description of the drawings
Fig. 1 is the structural representation of the embodiment of the present invention.
Embodiment
The present invention is described in further detail with reference to the accompanying drawings and examples：
Reference picture 1, using the re-liquefied system of natural gas vaporization gas of twin-stage mixed-refrigerant cycle, including heat exchanger
HX1, heat exchanger HX1 outlet c are connected with first order high temperature refrigerant compressor C6 entrances, first order high temperature refrigerant compressor
C6 is exported and the connection of the entrance of the 5th cooler 5, and the outlet of the 5th cooler 5 and second level high temperature refrigerant compressor C7 entrances connect
Connect, high temperature refrigerant compressor C7 outlets in the second level are connected with the entrance of the 6th cooler 6, and the 6th cooler 6 is exported and heat exchanger
HX1 entrance e connections, and the heat exchanger HX1 of entrance e connections outlet f are connected with high temperature refrigerant choke valve V2 entrances, high temperature
Refrigerant choke valve V2 outlets are connected with heat exchanger HX1 entrance d, and entrance d is connected with outlet c, constitutes high-temperature region hybrid refrigeration
Agent (MR2) is circulated.
After the low-pressure refrigerant vapor MR2-1 that first order high temperature refrigerant compressor C6 suctions are discharged from heat exchanger HX1, pressure
Maximum pressure is compressed into second level high temperature refrigerant compressor C7 after entering the cooling during rolling of the 5th cooler 5 after contracting, then
The refrigerant MR2-4 of high pressure, which enters in the 6th cooler 6, is cooled to environment temperature, and the refrigerant MR2-5 of high pressure is flowed into afterwards
Heat exchanger HX1 is too cold to state MR2-6 to be throttled in high temperature refrigerant choke valve V2, and flows back into heat exchanger HX1 for it
Cold is provided；High-pressure natural gas, high pressure low temperature mix refrigerant MR1 and the release of itself cooling procedure are absorbed in heat exchanger HX1
Heat, and by after gasification rewarming, the refrigerant MR2-1 of low pressure is sucked by first order high temperature refrigerant compressor C6, under
MR2 circulation.
Heat exchanger HX1 outlet a is connected with first order low-temperature refrigerant compressor C4 entrances, first order low-temperature refrigerant pressure
Contracting machine C4 outlets are connected with the entrance of the 3rd cooler 3, the outlet of the 3rd cooler 3 and second level low-temperature refrigerant compressor C5 entrances
Connection, second level low-temperature refrigerant compressor C5 outlets and the connection of the entrance of the 4th cooler 4, the outlet of the 4th cooler 4 and heat exchange
Device HX1 entrance g connections, and the heat exchanger HX1 of entrance g connections outlet h are connected with heat exchanger HX2 entrance m, and entrance m
The heat exchanger HX2 of connection outlet n is connected with low-temperature refrigerant choke valve V1 entrances, and low-temperature refrigerant choke valve V1 is exported with changing
Hot device HX2 entrance l connections, and the heat exchanger HX2 of entrance l connections outlet k are connected with heat exchanger HX1 entrance b, entrance b
Connected with heat exchanger HX1 outlet a, constitute low-temperature space mix refrigerant (MR1) circulation.
The low pressure refrigerant MR1-1 that first order low-temperature refrigerant compressor C4 suctions are discharged by heat exchanger HX1, after compression
MR1-2 enters in the 3rd cooler 3 is compressed into maximum pressure after cooling into second level low-temperature refrigerant compressor C5, then
The refrigerant MR1-4 of high pressure, which enters in the 4th cooler 4, is cooled to environment temperature, enters backflowed in heat exchanger HX1 afterwards
High-temperature region mix refrigerant MR2 precoolings, enter back into after being too cold in heat exchanger HX2 and to be saved in low-temperature refrigerant choke valve V1
Stream, and backflow and pass sequentially through heat exchanger HX2, heat exchanger HX1 and provide cold for it；Refrigerant is gasified totally in heat exchanger HX1
Rewarming is is sucked by first order low-temperature refrigerant compressor C4 after MR1-1, into the circulations of MR1 next time.
Heat exchanger HX1 outlet j is connected with heat exchanger HX2 entrance o, the heat exchanger HX2 connected with entrance o outlet p
It is connected with subcooler HX3 entrance s, the subcooler HX3 connected with entrance s outlet t and injector E0 main fluid entrances u connect
Connect, injector E0 driven fluid entrance v and storage tank BOG outlet is connected, and injector E0 outlet w and gas-liquid separator S0 enter
Mouth x connections, gas-liquid separator S0 liquid-phase outlet y and BOG choke valve V0 entrances are connected, BOG choke valves V0 outlets and LNG storage tank
Connection；The gaseous phase outlet z and subcooler HX3 of gas-liquid separator entrance r connections, the subcooler HX3 connected with entrance r outlet
Q is connected with first order BOG compressor C1 entrances, and first order BOG compressors C1 exports the entrance phase with second level BOG compressors C2
Even, second level BOG compressors C2 outlet and the entrance of the first cooler 1 are connected, the outlet of the first cooler 1 and the third level
BOG compressor C3 entrances are connected, and third level BOG compressors C3 outlets are connected with the entrance of the second cooler 2, and the second cooler 2 goes out
Mouth is connected with heat exchanger HX1 entrance i, and entrance i is connected with heat exchanger HX1 outlet j, so far constitutes the liquefaction of BOG ejector refrigerations
Circulation.
Low pressure BOG M0 from subcooler HX3 discharges are after multi-stage compression cooling during rolling, as normal temperature high voltage natural gas M5,
Heat exchanger HX1, heat exchanger HX2 is then sequentially entered to be cooled down and liquid by the cold that foregoing MR2 is circulated and MR1 circulations are provided respectively
Change, made afterwards into subcooler HX3 by after the low temperature BOG M10 supercoolings of backflowing from gas-liquid separator S0 into injector E0
For BOG of the main fluid M8 injections in storage tank, low temperature gas-fluid two-phase mixture M9 is produced in injector E0 outlets, is entered afterwards
Two-phase laminated flow in gas-liquid separator S0, gas part M10 backflows, and foregoing high-pressure natural gas M7, liquid are subcooled into subcooler HX3
Body portion is returned after BOG choke valves V0 throttling pressure regulation in storage tank.
Described heat exchanger HX1 and heat exchanger HX2 is Heat Exchangers, in heat exchanger HX1, high-temperature region hybrid refrigeration
Exchanged heat while agent, low-temperature space mix refrigerant and BOG；In heat exchanger HX2, low-temperature space mix refrigerant and BOG's
Exchanged heat simultaneously.
Because liquefied natural gas boiloff gas component is with methane (CH4) based on, described high-temperature region mix refrigerant (MR2)
It is made up of iso-butane, propane and ethane, described low-temperature space mix refrigerant (MR1) is made up of propane, ethene and methane；It is described
Cooler use water-cooling cooler, the temperature of each logistics outflow cooler is 30 DEG C.The heat exchanger HX1 and HX2 is
Each stream temperature of Heat Exchangers, its hot side and cold side channel arrival end and the port of export should be consistent.
High-temperature region mix refrigerant (MR2) circulation uses two stages of compression cooling during rolling, the high-temperature region mix refrigerant
(MR2) all condensations are realized in the 6th cooler 6, high temperature refrigerant choke valve V2, throttling are flowed into after being subcooled through heat exchanger HX1
To 0.105MPa, the two-phase fluid that temperature is less than -50 DEG C is obtained, heat exchanger HX1 gasification heat absorptions are flowed back into.The high-temperature region mixing
After refrigerant (MR2) is gasified totally in heat exchanger HX1 and is superheated to higher than 20 DEG C, by first order high temperature refrigerant compressor C6
Suction.
Low-temperature space mix refrigerant (MR1) circulation is similar to high-temperature region mixed-refrigerant cycle, equally using two stages of compression
Cooling during rolling, the low-temperature space mix refrigerant (MR1) of the high pressure is cooled to 30 DEG C in the 4th cooler 4, through heat exchanger
HX1 is cooled to -50 DEG C or so in advance, realizes and enters heat exchanger HX2 after partial condensation；The low-temperature space mix refrigerant (MR1) is being changed
Realized in hot device HX2 and enter low-temperature refrigerant choke valve V1 after all condensing and be subcooled, throttling to 0.105MPa obtains temperature low
In -120 DEG C of two-phase fluid, heat exchanger HX2 and HX1 gasification heat absorption are flowed back into successively, cold is provided for it；The low-temperature space is mixed
After conjunction refrigerant (MR1) is superheated to higher than 20 DEG C through heat exchanger HX1, sucked by first order low-temperature refrigerant compressor C4.
The re-liquefied circulations of BOG use three stage compression cooling during rolling, and BOG is compressed into high pressure, 30 are cooled in cooler
DEG C, it is cooled to -50 DEG C or so in advance through heat exchanger HX1, total condensation is realized in heat exchanger HX2 and is cooled to -120 DEG C excessively, through supercooling
Device HX3 is further too cold to less than -130 DEG C；The liquid phase BOG of the cryogenic high pressure enters injector, is used as main fluid injection
Low pressure BOG in storage tank；The two-phase fluid for exporting the low-temp low-pressure obtained in injector enters gas-liquid separator, wherein gas
Sucked after mutually cold is reclaimed in part through subcooler HX3 by first order BOG compressors C1, liquid phase part throttles through BOG choke valves V0
Returned after to 0.107MPa in storage tank.
The method calculated using flowsheeting illustrates the embodiment shown in Fig. 1, and the results are shown in Table 1.It is assumed that natural gas
Logistics is made up of pure methane, and the maximum pressure of natural gas circulation is 4MPa (i.e. third level BOG compressors C3 outlet pressure), is come
From natural gas boil-off gas (BOG) pressure of LNG storage tank be 0.107MP, temperature be -125 DEG C；Return storage tank gas pressure be
0.107MPa, temperature are -160.9 DEG C.High-temperature region mix refrigerant (MR2) is made up of iso-butane, propane and ethane, its mole point
Number is respectively 0.4697,0.3310 and 0.1993, and low-temperature space mix refrigerant (MR1) is made up of propane, ethene and methane, its
Molar fraction is respectively 0.1862,0.6906 and 0.1232.Those skilled in the art can determine that the enclosed mixed-refrigerant cycle
The composition of middle refrigerant, makes under the conditions of a variety of unstripped gas composition, pressure and temperature, natural gas vaporization gas is again
Wasted work amount needed for liquefaction flow path is minimum.Result of calculation shows that the pressure of required high-temperature region and low-temperature space mixed-refrigerant cycle is most
Height is no more than 2MPa.
The embodiment is further description made for the present invention, it is impossible to assert the embodiment of the present invention only
It is limited to this, for general technical staff of the technical field of the invention, without departing from the inventive concept of the premise, also
Some simple deduction or replace can be made, the present invention should be all considered as belonging to and determine patent by the claims submitted
Protection domain.
The embodiment major parameter of table 1
Claims (4)
1. using the re-liquefied system of natural gas vaporization gas of twin-stage mixed-refrigerant cycle, including heat exchanger HX1, its feature
It is：Heat exchanger HX1 outlet c is connected with first order high temperature refrigerant compressor C6 entrances, the compression of first order high temperature refrigerant
Machine C6 is exported and the connection of the entrance of the 5th cooler 5, and the outlet of the 5th cooler 5 and second level high temperature refrigerant compressor C7 entrances connect
Connect, high temperature refrigerant compressor C7 outlets in the second level are connected with the entrance of the 6th cooler 6, and the 6th cooler 6 is exported and heat exchanger
HX1 entrance e connections, and the heat exchanger HX1 of entrance e connections outlet f are connected with high temperature refrigerant choke valve V2 entrances, high temperature
Refrigerant choke valve V2 outlets are connected with heat exchanger HX1 entrance d, and entrance d is connected with outlet c, constitutes high-temperature region hybrid refrigeration
Agent (MR2) is circulated；
Heat exchanger HX1 outlet a is connected with first order low-temperature refrigerant compressor C4 entrances, first order low-temperature refrigerant compressor
C4 outlets are connected with the entrance of the 3rd cooler 3, and the outlet of the 3rd cooler 3 connects with second level low-temperature refrigerant compressor C5 entrances
Connect, second level low-temperature refrigerant compressor C5 outlets and the connection of the entrance of the 4th cooler 4, the 4th cooler 4 are exported and heat exchanger
HX1 entrance g connections, and the heat exchanger HX1 of entrance g connections outlet h are connected with heat exchanger HX2 entrance m, and entrance m connects
Logical heat exchanger HX2 outlet n is connected with low-temperature refrigerant choke valve V1 entrances, low-temperature refrigerant choke valve V1 outlets and heat exchange
Device HX2 entrance l connections, and the heat exchanger HX2 outlet k of entrance l connections are connected with heat exchanger HX1 entrance b, entrance b with
Heat exchanger HX1 outlet a connections, constitute low-temperature space mix refrigerant (MR1) circulation；
Heat exchanger HX1 outlet j is connected with heat exchanger HX2 entrance o, and entrance o connection heat exchanger HX2 outlet p and mistake
Cooler HX3 entrance s connections, the subcooler HX3 connected with entrance s outlet t and injector E0 main fluid entrance u connections, spray
Emitter E0 driven fluid entrance v and storage tank BOG outlet is connected, and injector E0 outlet w and gas-liquid separator S0 entrances x connect
Connect, gas-liquid separator S0 liquid-phase outlet y and BOG choke valve V0 entrances are connected, BOG choke valves V0 outlets are connected with LNG storage tank；
The gaseous phase outlet z and subcooler HX3 of gas-liquid separator entrance r connections, and the subcooler HX3 of entrance r connections outlet q and the
One-level BOG compressor C1 entrances are connected, and first order BOG compressors C1 outlets are connected with second level BOG compressors C2 entrance, the
Two BOG compressors C2 outlet and the entrance of the first cooler 1 are connected, outlet and the third level BOG compressors of the first cooler 1
C3 entrances are connected, and third level BOG compressors C3 outlets are connected with the entrance of the second cooler 2, and the second cooler 2 is exported and heat exchanger
HX1 entrance i is connected, and entrance i is connected with heat exchanger HX1 outlet j, so far constitutes BOG ejector refrigeration liquefaction cycles.
2. the re-liquefied system of natural gas vaporization gas of use twin-stage mixed-refrigerant cycle according to claim 1,
It is characterized in that：Described high-temperature region mix refrigerant includes iso-butane, propane and ethane, the low-temperature space mix refrigerant bag
Containing propane, ethene and methane.
3. the re-liquefied system of natural gas vaporization gas of use twin-stage mixed-refrigerant cycle according to claim 1,
It is characterized in that：Described high-temperature region mix refrigerant (MR2), which is recycled into before heat exchanger HX1, realizes all condensations, described
Low-temperature space mix refrigerant (MR1) realizes partial condensation before being recycled into heat exchanger HX2.
4. the re-liquefied system of natural gas vaporization gas of use twin-stage mixed-refrigerant cycle according to claim 1,
It is characterized in that：Described BOG ejector refrigerations liquefaction cycle realizes all liquefaction before subcooler HX3 is entered.
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| CN107726045A (en) * | 2017-09-29 | 2018-02-23 | 深圳市燃气集团股份有限公司 | A kind of BOG liquefaction recycling systems of liquefied natural gas |
| CN108489133A (en) * | 2018-03-13 | 2018-09-04 | 中国科学院理化技术研究所 | Multi-stage compression mixed working medium refrigerating/liquefying system |
| CN109404716A (en) * | 2018-11-27 | 2019-03-01 | 郑州大学 | A kind of re-liquefied coaxial linkage Jie formula system of gas station BOG |
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| CN113274951A (en) * | 2021-05-21 | 2021-08-20 | 济南隆凯能源科技有限公司 | Double-steam injection circulating hydrocarbon partial oxidation system and method |
| CN114017989A (en) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | LNG-BOG reliquefaction system and mixed refrigerant suitable for same |
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| CN107726045A (en) * | 2017-09-29 | 2018-02-23 | 深圳市燃气集团股份有限公司 | A kind of BOG liquefaction recycling systems of liquefied natural gas |
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| CN113274951A (en) * | 2021-05-21 | 2021-08-20 | 济南隆凯能源科技有限公司 | Double-steam injection circulating hydrocarbon partial oxidation system and method |
| CN113274951B (en) * | 2021-05-21 | 2022-12-20 | 济南隆凯能源科技有限公司 | Double-steam injection circulating hydrocarbon partial oxidation system and method |
| CN114017989A (en) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | LNG-BOG reliquefaction system and mixed refrigerant suitable for same |
| CN114017988A (en) * | 2021-12-01 | 2022-02-08 | 上海齐耀动力技术有限公司 | BOG (boil-off gas) reliquefaction circulation system for LNG (liquefied Natural gas) ship based on mixed working medium refrigeration technology |
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Application publication date: 20170915 |