CN107560321A - BOG is reclaimed and nitrogen gas liquefaction system and process - Google Patents
BOG is reclaimed and nitrogen gas liquefaction system and process Download PDFInfo
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- CN107560321A CN107560321A CN201710835492.XA CN201710835492A CN107560321A CN 107560321 A CN107560321 A CN 107560321A CN 201710835492 A CN201710835492 A CN 201710835492A CN 107560321 A CN107560321 A CN 107560321A
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Abstract
The invention discloses a kind of BOG recovery and nitrogen gas liquefaction system and process, the nitrogen prepared by LNG cold energy to PSA nitrogen-making devices is carried out two level cooling by the system makes it liquefy and store；In BOG liquefaction systems, BOG pressurizes through compressor and exchanged heat again with liquid nitrogen, makes its liquefaction, and liquid nitrogen absorbs heat gasification and is stored in nitrogen storage tank, purged available for yard；The BOG being liquefied enters defeated outside high-pressure pump or through expenditure and pressure, and into separator, the bottom storage of liquid phase injection LNG storage tank, gas phase enters BOG compression circulations.The inventive method solves the problems, such as that BOG recovery is difficult under the low outer throughput rate of LNG receiving stations, and meet the needs of yard low temperature purging process, it make use of LNG cold energy to improve efficiency of energy utilization, used the existing PSA equipments of making nitrogen in LNG station field to reduce equipment investment.
Description
Technical field
The present invention relates to LNG storages and the technical field of transport field, and in particular to a kind of BOG recovery and liquefaction of nitrogen system
System and process.
Background technology
As atmosphere polluting problem increasingly highlights, China is more urgent to the demand of clean energy resource.LNG (liquefied natural gas)
As a kind of accumulating form of this clean energy resource of natural gas, coastal cities combustion gas guarantee and peak regulation are widely used in.China LNG connects
Receive station and be distributed widely in each coastal cities, caused a large amount of BOG (flash steam) produce to the safety of receiving station in its running
It is raw to threaten.BOG is gases of the LNG by thermal evaporation formation, because insulation material is limited, unavoidably penetrates into heat from the external world, causes
LNG is by thermal evaporation.As heat is constantly attacked, the increase of gas phase quality, pressure vessel pressure-bearing increase, if can not hold reaching container
Release BOG will produce high risks to equipment before carrying pressure, and superpressure damage tank body occurs.Touched when gas-phase space reaches certain pressure
Relief valve is sent out, unnecessary flashed vapour in tank is immediately discharged to torch emptying burning.Large LNG yard BOG total amounts are larger, directly
Discharge causes the waste of the energy and the pollution of environment.
The BOG processing methods for having realized application in LNG receiving stations of China at present mainly have：
(1) direct compression process, i.e., BOG gases are carried out by high pressure compressed unit direct weighting to Trunk-line pressure
Outer defeated, the few flow of process equipment is simple, but process energy consumption is high, and security is poor.
(2) recondensation process, i.e. BOG gases are first pressurizeed by compressor, then the LNG with being pumped out in tank is mixed, by
LNG liquefaction BOG are subcooled, and through high-pressure pump two-stage pressurizing, are most sent into pipe network through gasifier gasification afterwards.The process energy consumption is far below straight
Compression method is connect, but outer defeated LNG stream amount limits BOG yield, for the uneven urban pipe network of downstream gas, when in use
LNG can not all condense BOG during gas low ebb, have to discharge.General BOG compressors not use by equipment, occurs needing under fortuitous event
Prolonged maintenance, a large amount of BOG will be wasted.
Novel B OG handling process based on Condensation Theory again has：
(1) mix refrigerant BOG recondensation process, i.e., will using kind of refrigeration cycle by the use of multicomponent lighter hydrocarbons as refrigerant
BOG condensation recovery, but the technique heat transmission equipment is more, and flow is complicated, and refrigerant proportioning needs extras.
(2) multistage compression BOG recondensation process, i.e., compression power consumption is reduced using multi-stage compression technology, and improves operation bullet
Property, but the technique can not handle the BOG recovery under stopping transportation operating mode, still have in the case where BOG largely produces the operating mode that for example unloads
There is limitation.
(3) the BOG recondensation process with expanding machine, expanding machine output shaft work is driven to supply using the high-pressure natural gas after gasification
To high-pressure pump, reach LNG superchargings while hardly consume the purpose of additional energy source, but this technique is because of its higher pressure limit pair
Process pipelines and supercharging equipment propose higher requirement, and the feasibility in the case where fluctuating operating mode needs further to be verified.
In view of the above state of the art, it is necessary to propose a kind of low energy consumption, in high yield, equipment investment is moderate, adapts to fluctuate
Operating mode simultaneously disclosure satisfy that the BOG auxiliary recovery methods of other demands of Large LNG yard realize energy-saving and emission-reduction, carry technological operation bullet
Property, high-energy source utilization ratio.
The content of the invention
It is an object of the invention to overcome the shortcomings of above-mentioned background technology, and provide a kind of energy-saving and emission-reduction, using energy source effect
The high BOG recovery of rate and nitrogen gas liquefaction system, present invention also offers a kind of BOG recovery and the process of liquefaction of nitrogen.
To achieve the above object, designed by the present invention in a kind of BOG recovery and nitrogen gas liquefaction system, including LNG storage tank, tank
Pump, the first LNG dispenser, after-condenser, the first LNG blenders, high-pressure pump, the second LNG dispenser, First Heat Exchanger, second
LNG blenders, LNG gasification device, PSA nitrogen-making devices, the first valve, nitrogen blender, nitrogen compressor, the second heat exchanger, nitrogen
Gas separating device, liquid nitrogen container, the second valve, BOG- liquid nitrogen heat exchanger, nitrogen pot, the 3rd valve, liquid nitrogen converter, BOG compressors,
BOG distributors, the 4th valve, the 5th valve, gas-liquid separator, the 6th valve；
Pump is arranged in LNG storage tank in the tank, the B of the first LNG dispenser of A outlets connection of pump in the tank3Import,
The B of first LNG dispenser1The D of the first LNG blenders of outlet connection1Import, the B of first LNG dispenser2Outlet connects
Meet the C of after-condenser1Import, the C of the after-condenser3The D of the first LNG blenders of outlet connection2Import, the first LNG are mixed
The outlet of clutch connects the E of the second LNG dispenser by high-pressure pump3Import, the E of second LNG dispenser1Outlet connection the
The F of one heat exchanger1Import, the F of the First Heat Exchanger2The G of the 2nd LNG blenders of outlet connection1Import；
The E of second LNG dispenser2The L of the second heat exchanger of outlet connection1Import, the L of second heat exchanger2Outlet
Connect the G of the 2nd LNG blenders2Import, the outlet of the 2nd LNG blenders are connected to the H of LNG gasification device1Import, it is described
The H of LNG gasification device2The extraneous gas line network of outlet connection；
The I of the PSA nitrogen-making devices1It is divided into two branch roads behind outlet, connects First Heat Exchanger by the first valve all the way
F3Import, another way is by the extraneous scavenging pipeline of the 6th valve connection；The F of the First Heat Exchanger4Outlet connection nitrogen mixes
The J of clutch1Import, the J of the nitrogen blender3The K of outlet connection nitrogen compressor1Import, the K of the nitrogen compressor2Go out
The L of mouth the second heat exchanger of connection3Import, the L of second heat exchanger4The M of outlet connection nitrogen separation device3Import, the nitrogen
The M of separator2Gaseous phase outlet connects the J of nitrogen blender2Import, the M of the nitrogen separation device1Liquid-phase outlet connects liquid nitrogen container
N1Import, the N of the liquid nitrogen container2It is divided into two branch roads behind outlet, connects BOG- liquid nitrogen heat exchangers by the second valve all the way
O3Import, another way connect the P of liquid nitrogen converter by the 3rd valve1Import；The O of the BOG- liquid nitrogen heat exchanger4Outlet connection
The Q of nitrogen pot1Import；
The R of the LNG storage tank1The import of outlet connection BOG compressors, the outlet connection BOG distribution of the BOG compressors
The T of device3Import, the T of the BOG distributors1The C of outlet connection after-condenser2Import；The T of the BOG distributors2Outlet connection
The O of BOG- liquid nitrogen heat exchangers1Import, the O of the BOG- liquid nitrogen heat exchanger2It is divided into two branch roads behind outlet, all the way by the 5th valve
The D of door the first LNG blenders of connection3Import, another way connect the V of gas-liquid separator by the 4th valve3Import, the gas-liquid
The V of separator1Gaseous phase outlet connects the import of BOG compressors, the V of the gas-liquid separator2Liquid-phase outlet connection LNG storage tank
R2Import.
In above-mentioned technical proposal, it also includes the first sea water pump, the second sea water pump, the H of the LNG gasification device3Import is led to
Cross the first sea water pump to be connected with seawater, the LNG gasification device is additionally provided with the H for discharging seawater4Outlet；The liquid nitrogen gasification
The P of device3Import is connected by the second sea water pump with seawater, and the liquid nitrogen converter is additionally provided with the P for discharging seawater4Import.
In above-mentioned technical proposal, the Q of the nitrogen pot2Outlet, the P of liquid nitrogen converter2Connect after outlet converges with scavenging pipeline
Connect.
In above-mentioned technical proposal, it also includes torch, and the air inlet of the torch passes through branch road and the R of LNG storage tank1Outlet
Connection.
In above-mentioned technical proposal, the L of second heat exchanger4Outlet and the M of nitrogen separation device3On pipeline between import
It is provided with first throttle valve.
In above-mentioned technical proposal, the V of the gas-liquid separator3Import and the O of BOG- liquid nitrogen heat exchangers2Pipe between outlet
Second throttle is provided with road.
Present invention also offers a kind of BOG recovery and the process of liquefaction of nitrogen, it comprises the following steps：
Step 1：The normal outer defeated flows of LNG：- 150~-100 DEG C in LNG storage tank, 115kPa BOG is through BOG compressors
0.5~0.9MPa is pressurized to, then is divided into two-way through BOG distributors, now the only T of BOG distributors1Outlet, BOG enter
The C of after-condenser2Import, while it is pressurized to the B that 0.5~0.9MPa supercooling LNG passes through the first LNG dispenser through pump in tank2Go out
Mouth enters the C of after-condenser1Import, BOG are contacted, mixed and are condensed into liquid with supercooling LNG in after-condenser, and lime set is led to
Cross the C of after-condenser3D of the outlet into the first LNG blenders2Import and the B by the first LNG dispenser1Outlet outflow
LNG converges, and is sent into the import of high-pressure pump, through high-pressure pump be pressurized to 9MPa, -153 DEG C, be divided into two-way through the second LNG dispenser, one
Road will be nitrogen precooled through First Heat Exchanger, and LNG temperature rises to -149.5 DEG C, and another way is through the second heat exchanger by liquefaction of nitrogen, LNG
Temperature rises to -30.6 DEG C, and it is natural that two-way LNG is sent into LNG gasification device with seawater to make heat exchange gasification after the mixing of the 2nd LNG blenders
Gas enters gas line network；H of the seawater through the supercharging of the first sea water pump into LNG gasification device3Import, through LNG gasification after being exchanged heat with LNG
The H of device4Outlet discharge；
Step 2：Liquefaction of nitrogen stores flow：20~25 DEG C made from PSA nitrogen-making devices, 0.6~0.7MPa nitrogen enters
Enter First Heat Exchanger to exchange heat with -153 DEG C, 9MPa LNG, precooling is cooled to -150 DEG C, then with the M of nitrogen separation device2Gas phase
Outlet outflow -175 DEG C, 0.69MPa low temperature nitrogen mixing temperature be down to -160 DEG C, be pressurized to through nitrogen compressor
2.95MPa, -85 DEG C, exchanged heat into the second heat exchanger and -153 DEG C, 9MPa LNG, be cooled to -150 DEG C, then through first throttle
Valve be decompressed to 0.69MPa, -175 DEG C, flow into nitrogen separation device separate liquid phase, through nitrogen separation device separation after liquid nitrogen enter
Liquid nitrogen container stores, and the low temperature nitrogen after the separation of nitrogen separation device converges with the nitrogen after First Heat Exchanger precooling in nitrogen blender
Conjunction enters nitrogen compressor and carries out nitrogen compression circulation, continuously utilizes LNG cold liquefaction nitrogen；
Step 3：BOG liquefaction is outer defeated and returns tank flow：- 150~-100 DEG C in LNG storage tank, 115kPa BOG is through BOG
Compressor boost is divided into two-way to 0.5~0.9MPa, then through BOG distributors, is carried out all the way into after-condenser described in step 1
The normal outer defeated flows of LNG；Another way enters BOG- liquid nitrogen heat exchangers, -175 DEG C with liquid nitrogen container outflow, 0.69MPa liquid nitrogen changes
Heat is cooled to -148 DEG C of BOG lime sets, and -40 DEG C of nitrogen temperature, 0.68MPa enter nitrogen pot after liquid nitrogen gasification, and BOG lime sets are passed through
The O of BOG- liquid nitrogen heat exchangers2Outlet is divided into two-way, and the LNG being sent into all the way through the 5th valve described in high-pressure pump progress step 1 is normal
Outer defeated flow, another way enter gas-liquid separator through second throttle decompression, and the liquid phase after gas-liquid separator separates flows into LNG
In storage tank, the gas phase after gas-liquid separator separates enters the import of BOG compressors, continuously outside progress BOG liquefaction
Defeated and time tank.
In above-mentioned technical proposal, in the step 1, the distribution of the second LNG dispenser enters First Heat Exchanger, the second heat exchanger
LNG mass ratioes be 1:70~72.
In above-mentioned technical proposal, nitrogen sweeping process is also included in the step 2, the nitrogen of the nitrogen sweeping process comes
Source is three parts, and Part I is that nitrogen caused by PSA nitrogen-making devices enters scavenging pipeline through the 6th valve；Part II is liquid
Liquid nitrogen in nitrogen tank passes through the 3rd valve, then enters scavenging pipeline after liquid nitrogen converter gasification is nitrogen；Part III is nitrogen
Nitrogen in gas tank is directly entered scavenging pipeline.
In above-mentioned technical proposal, if the step 1 and step 2 can not be realized, the R of LNG storage tank1Outlet will be with torch
Air inlet connect, BOG will be fed into torch emptying burning.
Compared with prior art, the invention has the advantages that：
First, the present invention utilizes " cold energy " that LNG more than needed is carried by PSA (pressure-variable adsorption separation) nitrogen caused by nitrogen-making device
Gas liquefaction condenses, and is stored in standby in liquid nitrogen container, and nitrogen exchanges heat by one-level precooling and LNG, is pressurized through nitrogen compressor, then with
LNG carries out heat exchange and realizes that two level cools down, and produces temperature drop by throttling, and separate low temperature liquid nitrogen through separator stores into storage tank；
Separator nitrogen and the nitrogen of one-level precooling, which converge to compress into nitrogen, to be circulated, and when the outer throughput rates of LNG are low or BOG yields are big, is adjusted
Take the low temperature liquid nitrogen in liquid nitrogen container to be used for BOG liquefaction condensations, and the gas nitrogen after heat exchange is stored in nitrogen storage tank；Condense BOG
It is outer defeated through high-pressure pump supercharging again, or LNG pressure stores are decompressed to through choke valve, separate lime set by separator notes from tank bottom
Enter storage, gas phase BOG returns to gas phase house steward and enters BOG compression circulations, takes full advantage of the PSA that domestic LNG station field generally possesses
Swing adsorption nitrogen producing apparatus, this causes the equipment investment needed for yard process modification to be reduced.
Second, the nitrogen prepared by LNG cold energy to PSA nitrogen-making devices is carried out two level cooling by the present invention makes its liquefaction simultaneously
Store；In BOG liquefaction systems, BOG pressurizes through compressor and exchanged heat again with liquid nitrogen, makes its liquefaction, and liquid nitrogen absorbs heat gas
Change is stored in nitrogen storage tank, is purged available for yard；The BOG being liquefied enters defeated or through expenditure and pressure outside high-pressure pump, enters
Enter separator, the bottom storage of liquid phase injection LNG storage tank, gas phase enters BOG compression circulations.The inventive method solves LNG receiving stations
The problem of BOG recovery is difficult under low outer throughput rate, and the needs of yard low temperature purging process are met, it make use of LNG cold energy to improve
Efficiency of energy utilization, has used the existing PSA equipments of making nitrogen in LNG station field to reduce equipment investment.
Third, the cool storage medium that uses of the present invention is inert nitrogen gas, compared to the refrigerant of light hydrocarbon mixture class,
Compression in heat-exchanging process with hardly bringing danger；And using nitrogen-liquid nitrogen as cool storage medium rather than simple nitrogen,
Cool storage medium total amount can be reduced using its latent heat rather than sensible heat.
Fourth, the storage and discharge of liquid nitrogen of the present invention, nitrogen will not cause greenhouse effects and environmental pollution, compare alkane
Class has the characteristic of clean environment firendly with fluorochlorohydrocarbon class refrigerating medium；
Fifth, the BOG and liquefaction of nitrogen technique in the present invention are simple, cost is cheap, easy to operate, and combines yard nitrogen
The demand of gas purging process, without outer enough liquid nitrogen again so that yard technical process has obtained integrated.
Sixth, the present invention adapts to fluctuate operating mode, cold more than needed is being stored with gas peak, released cold with gas low ebb
Put, realize the condensation recovery under BOG high load capacities, reduce energy waste and environmental pollution.
Brief description of the drawings
Fig. 1 is a kind of BOG recovery and the structural representation of nitrogen gas liquefaction system；
Embodiment
Describe the performance of the present invention in detail with reference to case study on implementation, but they do not form the limit to the present invention
It is fixed, it is only for example.Simultaneously by illustrating that advantages of the present invention will become clearer and be readily appreciated that.
Pump 2, first in a kind of BOG recovery of the present invention as shown in Figure 1 and nitrogen gas liquefaction system, including LNG storage tank 1, tank
LNG dispenser 3, after-condenser 4, the first LNG blenders 5, high-pressure pump 6, the second LNG dispenser 7, First Heat Exchanger 8, second
LNG blenders 9, LNG gasification device 10, PSA nitrogen-making devices 11, the first valve 12, nitrogen blender 13, nitrogen compressor 14,
Two heat exchangers 15, nitrogen separation device 17, liquid nitrogen container 18, the second valve 19, BOG- liquid nitrogen heat exchanger 20, nitrogen pot 21, the 3rd valve
Door 22, liquid nitrogen converter 23, BOG compressors 24, BOG distributors 25, the 4th valve 26, the 5th valve 27, gas-liquid separator 29,
6th valve 33, torch 30；
Pump 2 is arranged in LNG storage tank 1 in the tank, the first LNG dispenser 3 of connection of A outlets 2.1 of pump 2 in the tank
B3Import 3.3, the B of first LNG dispenser 31The D of the first LNG blenders 5 of the connection of outlet 3.11Import 5.1, described first
The B of LNG dispenser 32The C of the connection of outlet 3.2 after-condenser 41Import 4.1, the C of the after-condenser 43The connection of outlet 4.3 first
The D of LNG blenders 52Import 5.2, the outlet of the first LNG blenders 5 connect the second LNG dispenser 7 by high-pressure pump 6
E3Import 7.3, the E of second LNG dispenser 71The F of the connection of outlet 7.1 First Heat Exchanger 81Import 8.1, first heat exchange
The F of device 82The G of the 2nd LNG blenders 9 of the connection of outlet 8.21Import 9.1；
The E of second LNG dispenser 72The L of second heat exchanger 15 of the connection of outlet 7.21Import 15.1, second heat exchange
The L of device 152The G of the 2nd LNG blenders 9 of the connection of outlet 15.22Import 9.2, the outlet of the 2nd LNG blenders 9 are connected to
The H of LNG gasification device 101Import 10.1, the H of the LNG gasification device 102The extraneous gas line network 35 of the connection of outlet 10.2；
The I of the PSA nitrogen-making devices 111It is divided into two branch roads behind outlet 11.1, all the way by the first valve 12 connection the
The F of one heat exchanger 83Import 8.3, another way connect the scavenging pipeline 34 in the external world by the 6th valve 33；The First Heat Exchanger 8
F4The J of the connection nitrogen blender of outlet 8.4 131Import 13.1, the J of the nitrogen blender 133The connection of outlet 13.3 nitrogen pressure
The K of contracting machine 141Import 14.1, the K of the nitrogen compressor 142The L of second heat exchanger 15 of the connection of outlet 14.23Import 15.3, institute
State the L of the second heat exchanger 154The M of the connection nitrogen separation device of outlet 15.4 173Import 17.3, the L of second heat exchanger 154Go out
The M of mouth 15.4 and nitrogen separation device 173First throttle valve 16, the nitrogen separation device are provided with pipeline between import 17.3
17 M2Gaseous phase outlet 17.2 connects the J of nitrogen blender 132Import 13.2, the M of the nitrogen separation device 171Liquid-phase outlet
The N of 17.1 connection liquid nitrogen containers 181Import 18.1, the N of the liquid nitrogen container 182It is divided into two branch roads behind outlet 18.2, all the way by the
The O of two valves 19 connection BOG- liquid nitrogen heat exchanger 203Import 20.3, another way is by the 3rd valve 22 connection liquid nitrogen converter 23
P1The O of BOG- liquid nitrogen heat exchanger 20 described in import 23.14The Q of the connection of outlet 20.4 nitrogen pot 211Import 21.1, the nitrogen
The Q of tank 212Outlet 21.2, the P of liquid nitrogen converter 232Outlet 23.2 is connected after converging with scavenging pipeline 34, the liquid nitrogen storage tank 18
Outlet streams need to flow to distinct device according to yard, when needing the liquefaction for BOG to supplement cold, open the second valve 19 and flow
To BOG- liquid nitrogen heat exchangers, stored for future use after gasification into nitrogen storage tank 21；When needing a large amount of nitrogen to be used for yard purging, open
Open the liquid nitrogen of the 3rd valve 22 and flow to liquid nitrogen converter 23, realize that Quick-gasifying supplements Nitrogen source gases, flow to blow line.The liquid
Nitrogen storage tank 18, the tank of nitrogen storage tank 21 hold need according to scale of station and BOG yields, purging with nitrogen amount be designed calculating with
Meet different scales LNG process requirements.
The R of the LNG storage tank 11The import of the connection BOG compressors of outlet 1.1 24, the outlet of the BOG compressors 24 connect
Meet the T of BOG distributors 253Import 25.3, the T of the BOG distributors 251The C of the connection of outlet 25.1 after-condenser 42Import 4.2；
The T of the BOG distributors 252The O of the connection BOG- liquid nitrogen heat exchanger of outlet 25.2 201Import 20.1, the BOG- liquid nitrogen heat exchanger
20 O2It is divided into two branch roads behind outlet 20.2, connects the D of the first LNG blenders 5 by the 5th valve 27 all the way3Import 5.3,
Another way connects the V of gas-liquid separator 29 by the 4th valve 263Import 29.3, the V of the gas-liquid separator 293Import 29.3
With the O of BOG- liquid nitrogen heat exchanger 202Second throttle 28, the gas-liquid separator 29 are provided with pipeline between outlet 20.2
V1Gaseous phase outlet 29.1 connects the import of BOG compressors 24, the V of the gas-liquid separator 292Liquid-phase outlet 29.2 connects LNG
The R of storage tank 12Import 1.2, the air inlet of the torch 30 pass through branch road and the R of LNG storage tank 11The connection of outlet 1.1.
In above-mentioned technical proposal, in addition to the first sea water pump 31, the second sea water pump 32, the H of the LNG gasification device 103Enter
Mouth 10.3 is connected by the first sea water pump 31 with seawater, and the LNG gasification device 10 is additionally provided with the H for discharging seawater4Outlet
10.4；The P of the liquid nitrogen converter 233Import 23.3 is connected by the second sea water pump 32 with seawater, the liquid nitrogen converter 23
It is additionally provided with the P for discharging seawater4Import 23.4.
BOG recovery of the present invention and the process of liquefaction of nitrogen, it comprises the following steps：
Step 1：The normal outer defeated flows of LNG：- 150~-100 DEG C in LNG storage tank 1,115kPa BOG is through BOG compressors
24 are pressurized to 0.5~0.9MPa, then divide through BOG distributors 25 for two-way, now the only T of BOG distributors 251Outlet 25.1 connects
Logical, BOG enters the C of after-condenser 42Import 4.2, while 0.5~0.9MPa supercooling LNG is pressurized to by through pump in tank 2
The B of one LNG dispenser 32Outlet 3.2 enters the C of after-condenser 41Import 4.1, BOG are carried out with supercooling LNG in after-condenser 4
Contact, mix and be condensed into liquid (its saturated vapour pressure need to meet the necessary NPSH requirement of high pressure pump inlet), lime set passes through
The C of after-condenser 43Outlet 4.3 enters the D of the first LNG blenders 52The import 5.2 and B by the first LNG dispenser 31Outlet
3.1 outflow LNG converge, be sent into high-pressure pump 6 import, through high-pressure pump 6 be pressurized to 9MPa, -153 DEG C, through the second LNG dispenser
7 points are two-way, all the way will be nitrogen precooled through First Heat Exchanger 8, and LNG temperature rises to -149.5 DEG C, and another way is through the second heat exchanger
Liquefaction of nitrogen, LNG temperature are risen to -30.6 DEG C by 15, and (distribution of the second LNG dispenser 7 enters First Heat Exchanger 8, the second heat exchanger
15 LNG mass ratioes are 1:70~72, first order cooling institute chilling requirement is smaller, and second level cooling nitrogen undergoes phase transition latent heat consumption
Cold is more), two-way LNG is sent into LNG gasification device 10 after the mixing of the 2nd LNG blenders 9 and gasifies to enter for natural gas with seawater to make heat exchange
Enter gas line network 35；H of the seawater through the supercharging of the first sea water pump 31 into LNG gasification device 103Import 10.3, passed through after being exchanged heat with LNG
The H of LNG gasification device 104The discharge of outlet 10.4；
Step 2：Liquefaction of nitrogen stores flow：20~25 DEG C, 0.6~0.7MPa nitrogen made from PSA nitrogen-making devices 11
The LNG that (oxygen content is less than 1%) enters First Heat Exchanger 8 and -153 DEG C, 9MPa exchanges heat, and precooling is cooled to -150 DEG C, then
With the M of nitrogen separation device 172Gaseous phase outlet 17.2 flow out -175 DEG C, 0.69MPa low temperature nitrogen mixing temperature be down to -160
DEG C, through nitrogen compressor 14 be pressurized to 2.95MPa, -85 DEG C, the LNG into the second heat exchanger 15 and -153 DEG C, 9MPa exchanges heat,
Be cooled to -150 DEG C, then through first throttle valve 16 be decompressed to 0.69MPa, -175 DEG C, flow into nitrogen separation device 17 and separate liquid phase,
Liquid nitrogen after the separation of nitrogen separation device 17 stores into liquid nitrogen container 18, nitrogen separation device 17 separate after low temperature nitrogen and through the
Nitrogen after the precooling of one heat exchanger 8 converges into nitrogen compressor 14 in nitrogen blender 13 carries out nitrogen compression circulation, continuously
Constantly utilize LNG cold liquefaction nitrogen；
Step 3：BOG liquefaction is outer defeated and returns tank flow：- 150~-100 DEG C in LNG storage tank 1,115kPa BOG is through BOG
Compressor 24 is pressurized to 0.5~0.9MPa, then divides through BOG distributors 25 for two-way, carries out step 1 into after-condenser 4 all the way
The normal outer defeated flows of described LNG；Another way enters BOG- liquid nitrogen heat exchanger 20, with liquid nitrogen container 18 flow out -175 DEG C,
0.69MPa liquid nitrogen heat exchange is cooled to -148 DEG C of BOG lime sets, while pressure need to meet NPSH (the required vapour of high pressure pump inlet
Lose surplus) (NPSH is 0.1MPa in this example) is required, -40 DEG C of nitrogen temperature, 0.68MPa enter nitrogen pot after liquid nitrogen gasification
21, BOG lime sets pass through the O of BOG- liquid nitrogen heat exchanger 20220.2 points of outlet is two-way, is sent into high-pressure pump through the 5th valve 27 all the way
6 carry out the normal outer defeated flows of LNG described in step 1, and another way enters gas-liquid separator 29 through the decompression of second throttle 28, through gas
Liquid phase after liquid/gas separator 29 separates is flowed into LNG storage tank 1, and the gas phase after the separation of gas-liquid separator 29 enters BOG compressors
24 import, continuously carry out defeated outside BOG liquefaction and return tank, wherein consumption liquid nitrogen is with the mass ratio for condensing BOG
2.2~2.3 (outer defeated after BOG condensations)：2.6~2.7 (depressurizing back tank after BOG condensations).
In above-mentioned technical proposal, nitrogen sweeping process is also included in the step 2, the nitrogen of the nitrogen sweeping process comes
Source is three parts, and Part I is that nitrogen caused by PSA nitrogen-making devices 11 enters scavenging pipeline 34 through the 6th valve 33；Second
It is divided into the liquid nitrogen in liquid nitrogen container 18 and passes through the 3rd valve 22, then enters scavenging pipeline after the gasification of liquid nitrogen converter 23 is nitrogen
34；Part III is that the nitrogen in nitrogen pot 21 is directly entered scavenging pipeline 34.Three of the above nitrogen gas source complements one another, no elder generation
Order afterwards.If the step 1 and step 2 can not be realized, the R of LNG storage tank 11Outlet 1.1 connects the air inlet with torch 30
Logical, BOG will be fed into torch emptying burning.
The present invention utilizes " cold energy " that LNG more than needed is carried by PSA (pressure-variable adsorption separation) Nitrogen Headspace caused by nitrogen-making device
Change condensation, be stored in standby in liquid nitrogen container, nitrogen exchanges heat by one-level precooling and LNG, is pressurized through nitrogen compressor, then with LNG
Carry out heat exchange and realize that two level cools down, and temperature drop is produced by throttling, separate low temperature liquid nitrogen through separator stores into storage tank；Separation
Device nitrogen and the nitrogen of one-level precooling, which converge to compress into nitrogen, to be circulated, and when the outer throughput rates of LNG are low or BOG yields are big, transfers liquid
Low temperature liquid nitrogen in nitrogen tank is used for BOG liquefaction condensations, and the gas nitrogen after heat exchange is stored in nitrogen storage tank；Condensation BOG is passed through again
High-pressure pump supercharging is outer defeated, or is decompressed to LNG pressure stores through choke valve, and separate lime set by separator injects storage from tank bottom
Deposit, gas phase BOG returns to gas phase house steward and enters BOG compression circulations, takes full advantage of the PSA transformations that domestic LNG station field generally possesses
Adsorption nitrogen making device, this causes the equipment investment needed for yard process modification to be reduced.
More than, it is only embodiment of the invention, it is noted that any those skilled in the art are in this hair
In bright disclosed technical scope, the change or replacement that can readily occur in should be all included within the scope of the present invention.
Claims (10)
1. pump (2) in a kind of BOG recovery and nitrogen gas liquefaction system, including LNG storage tank (1), tank, the first LNG dispenser (3), again
Condenser (4), the first LNG blenders (5), high-pressure pump (6), the second LNG dispenser (7), First Heat Exchanger (8), the 2nd LNG are mixed
Clutch (9), LNG gasification device (10), PSA nitrogen-making devices (11), the first valve (12), nitrogen blender (13), nitrogen compressor
(14), the second heat exchanger (15), nitrogen separation device (17), liquid nitrogen container (18), the second valve (19), BOG- liquid nitrogen heat exchangers
(20), nitrogen pot (21), the 3rd valve (22), liquid nitrogen converter (23), BOG compressors (24), BOG distributors (25), the 4th
Valve (26), the 5th valve (27), gas-liquid separator (29), the 6th valve (33)；
Pump (2) is arranged in LNG storage tank (1) in the tank, A outlets (2.1) connection the first LNG distribution of pump (2) in the tank
The B of device (3)3Import (3.3), the B of first LNG dispenser (3)1Export the D that (3.1) connect the first LNG blenders (5)1Enter
Mouth (5.1), the B of first LNG dispenser (3)2Export the C of (3.2) connection after-condenser (4)1Import (4.1), it is described cold again
The C of condenser (4)3Export the D that (4.3) connect the first LNG blenders (5)2Import (5.2), the first LNG blenders (5) go out
Mouth connects the E of the second LNG dispenser (7) by high-pressure pump (6)3Import (7.3), the E of second LNG dispenser (7)1Outlet
(7.1) F of First Heat Exchanger (8) is connected1Import (8.1), the F of the First Heat Exchanger (8)2Export (8.2) and connect the 2nd LNG
The G of blender (9)1Import (9.1)；
The E of second LNG dispenser (7)2Export the L that (7.2) connect the second heat exchanger (15)1Import (15.1), described second
The L of heat exchanger (15)2Export the G that (15.2) connect the 2nd LNG blenders (9)2Import (9.2), the 2nd LNG blenders (9)
Outlet be connected to the H of LNG gasification device (10)1Import (10.1), the H of the LNG gasification device (10)2It is outer to export (10.2) connection
The gas line network (35) on boundary；
The I of the PSA nitrogen-making devices (11)1It is divided into two branch roads behind outlet (11.1), all the way by the first valve (12) connection the
The F of one heat exchanger (8)3Import (8.3), another way is by the extraneous scavenging pipeline (34) of the 6th valve (33) connection；Described
The F of one heat exchanger (8)4Export the J of (8.4) connection nitrogen blender (13)1Import (13.1), the nitrogen blender (13)
J3Export the K of (13.3) connection nitrogen compressor (14)1Import (14.1), the K of the nitrogen compressor (14)2Export (14.2)
Connect the L of the second heat exchanger (15)3Import (15.3), the L of second heat exchanger (15)4Export (15.4) connection nitrogen separation
The M of device (17)3Import (17.3), the M of the nitrogen separation device (17)2Gaseous phase outlet (17.2) connection nitrogen blender (13)
J2Import (13.2), the M of the nitrogen separation device (17)1The N of liquid-phase outlet (17.1) connection liquid nitrogen container (18)1Import (18.1),
The N of the liquid nitrogen container (18)2It is divided into two branch roads behind outlet (18.2), is changed all the way by the second valve (19) connection BOG- liquid nitrogen
The O of hot device (20)3Import (20.3), another way connect the P of liquid nitrogen converter (23) by the 3rd valve (22)1Import (23.1)；
The O of the BOG- liquid nitrogen heat exchanger (20)4Export the Q of (20.4) connection nitrogen pot (21)1Import (21.1)；
The R of the LNG storage tank (1)1Export the import of (1.1) connection BOG compressors (24), the outlet of the BOG compressors (24)
Connect the T of BOG distributors (25)3Import (25.3), the T of the BOG distributors (25)1Export (25.1) connection after-condenser (4)
C2Import (4.2)；The T of the BOG distributors (25)2Export the O of (25.2) connection BOG- liquid nitrogen heat exchanger (20)1Import
(20.1), the O of the BOG- liquid nitrogen heat exchanger (20)2It is divided into two branch roads behind outlet (20.2), all the way by the 5th valve
(27) D of the first LNG blenders (5) is connected3Import (5.3), another way is by the 4th valve (26) connection gas-liquid separator
(29) V3Import (29.3), the V of the gas-liquid separator (29)1Gaseous phase outlet (29.1) connection BOG compressor (24) is entered
Mouthful, the V of the gas-liquid separator (29)2The R of liquid-phase outlet (29.2) connection LNG storage tank (1)2Import (1.2).
2. BOG recovery according to claim 1 and nitrogen gas liquefaction system, it is characterised in that：Also include the first sea water pump
(31), the second sea water pump (32), the H of the LNG gasification device (10)3Import (10.3) is connected by the first sea water pump (31) and seawater
Connect, the LNG gasification device (10) is additionally provided with the H for discharging seawater4Export (10.4)；The P of the liquid nitrogen converter (23)3
Import (23.3) is connected by the second sea water pump (32) with seawater, and the liquid nitrogen converter (23) is additionally provided with for discharging seawater
P4Import (23.4).
3. BOG recovery according to claim 2 and nitrogen gas liquefaction system, it is characterised in that：The Q of the nitrogen pot (21)2Go out
Mouth (21.2), the P of liquid nitrogen converter (23)2Outlet (23.2) is connected after converging with scavenging pipeline (34).
4. BOG recovery according to claim 3 and nitrogen gas liquefaction system, it is characterised in that：It also includes torch (30), institute
The air inlet for stating torch (30) passes through branch road and the R of LNG storage tank (1)1Export (1.1) connection.
5. BOG recovery according to claim 4 and nitrogen gas liquefaction system, it is characterised in that：Second heat exchanger (15)
L4Export (15.4) and the M of nitrogen separation device (17)3First throttle valve (16) is provided with pipeline between import (17.3).
6. BOG recovery according to claim 5 and nitrogen gas liquefaction system, it is characterised in that：The gas-liquid separator (29)
V3Import (29.3) and the O of BOG- liquid nitrogen heat exchanger (20)2Second throttle is provided with pipeline between outlet (20.2)
(28)。
7. a kind of utilize BOG recovery described in claim 6 and the process of liquefaction of nitrogen, it is characterised in that it includes as follows
Step：
Step 1：The normal outer defeated flows of LNG：- 150~-100 DEG C in LNG storage tank (1), 115kPa BOG is through BOG compressors
(24) 0.5~0.9MPa is pressurized to, then is divided into two-way through BOG distributors (25), now the only T of BOG distributors (25)1Outlet
(25.1) connect, BOG enters the C of after-condenser (4)2Import (4.2), while it is pressurized to 0.5~0.9MPa's through pump in tank (2)
Bs of the LNG by the first LNG dispenser (3) is subcooled2Export the C that (3.2) enter after-condenser (4)1Import (4.1), BOG and supercooling
LNG is contacted, mixed and is condensed into liquid, the C that lime set passes through after-condenser (4) in after-condenser (4)3Outlet (4.3) is entered
Enter the D of the first LNG blenders (5)2Import (5.2) and the B by the first LNG dispenser (3)1The LNG for exporting (3.1) outflow converges
Close, be sent into high-pressure pump (6) import, through high-pressure pump (6) be pressurized to 9MPa, -153 DEG C, be divided into two through the second LNG dispenser (7)
Road, all the way will be nitrogen precooled through First Heat Exchanger (8), and LNG temperature rises to -149.5 DEG C, and another way will through the second heat exchanger (15)
Liquefaction of nitrogen, LNG temperature rise to -30.6 DEG C, and two-way LNG is sent into LNG gasification device (10) after the mixing of the 2nd LNG blenders (9)
Enter gas line network (35) with seawater to make heat exchange gasification for natural gas；Seawater enters LNG gasification device through the first sea water pump (31) supercharging
(10) H3Import (10.3), the H through LNG gasification device (10) after being exchanged heat with LNG4Export (10.4) discharge；
Step 2：Liquefaction of nitrogen stores flow：20~25 DEG C made from PSA nitrogen-making devices (11), 0.6~0.7MPa nitrogen enters
Enter First Heat Exchanger (8) to exchange heat with -153 DEG C, 9MPa LNG, precooling is cooled to -150 DEG C, then with nitrogen separation device (17)
M2Gaseous phase outlet (17.2) outflow -175 DEG C, 0.69MPa low temperature nitrogen mixing temperature be down to -160 DEG C, through nitrogen compressor
(14) be pressurized to 2.95MPa, -85 DEG C, exchanged heat into the second heat exchanger (15) and -153 DEG C, 9MPa LNG, be cooled to -150
DEG C, then through first throttle valve (16) be decompressed to 0.69MPa, -175 DEG C, flow into nitrogen separation device (17) separate liquid phase, through nitrogen
Liquid nitrogen after separator (17) separation enters liquid nitrogen container (18) and stored, low temperature nitrogen after nitrogen separation device (17) separation and through the
Nitrogen after one heat exchanger (8) precooling converges into nitrogen compressor (14) progress nitrogen compression in nitrogen blender (13) to follow
Ring, continuously utilize LNG cold liquefaction nitrogen；
Step 3：BOG liquefaction is outer defeated and returns tank flow：- 150~-100 DEG C in LNG storage tank (1), 115kPa BOG presses through BOG
Contracting machine (24) is pressurized to 0.5~0.9MPa, then is divided into two-way through BOG distributors (25), is walked all the way into after-condenser (4)
It is rapid 1) described in the normal outer defeated flows of LNG；Another way enters BOG- liquid nitrogen heat exchanger (20), and -175 with liquid nitrogen container (18) outflow
DEG C, the heat exchange of 0.69MPa liquid nitrogen be cooled to -148 DEG C of BOG lime sets, -40 DEG C of nitrogen temperature, 0.68MPa enter after liquid nitrogen gasification
Nitrogen pot (21), BOG lime sets pass through the O of BOG- liquid nitrogen heat exchanger (20)2Outlet (20.2) is divided into two-way, all the way through the 5th valve
(27) be sent into high-pressure pump (6) and carry out normal outer defeated flows of LNG described in step 1, another way through second throttle (28) depressurize into
Enter gas-liquid separator (29), the liquid phase after gas-liquid separator (29) separation is flowed into LNG storage tank (1), through gas-liquid separator
(29) gas phase after separating enters the import of BOG compressors (24), continuously carries out defeated outside BOG liquefaction and returns tank.
8. BOG recovery according to claim 7 and the method for liquefaction of nitrogen, it is characterised in that also include in the step 2
Nitrogen sweeping process, the nitrogen gas source of the nitrogen sweeping process is three parts, and Part I produces for PSA nitrogen-making devices (11)
Nitrogen enter scavenging pipeline (34) through the 6th valve (33)；Part II is that the liquid nitrogen in liquid nitrogen container (18) passes through the 3rd valve
(22), then after liquid nitrogen converter (23) gasification is nitrogen scavenging pipeline (34) is entered；Part III is in nitrogen pot (21)
Nitrogen is directly entered scavenging pipeline (34).
9. BOG recovery according to claim 7 and the method for liquefaction of nitrogen, it is characterised in that in the step 1, second
LNG dispenser (7) distribution enters First Heat Exchanger (8), the LNG mass ratioes of the second heat exchanger (15) are 1:70~72.
10. BOG recovery according to claim 9 and the method for liquefaction of nitrogen, it is characterised in that if the step 1 and step
Rapid 2 when can not realize, the R of LNG storage tank (1)1Exporting (1.1) will be connected with the air inlet of torch (30), and BOG is put into torch
Air-fuel is burnt.
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