CN103343881A - Technology of BOG recovery and device thereof - Google Patents
Technology of BOG recovery and device thereof Download PDFInfo
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- CN103343881A CN103343881A CN2013102437085A CN201310243708A CN103343881A CN 103343881 A CN103343881 A CN 103343881A CN 2013102437085 A CN2013102437085 A CN 2013102437085A CN 201310243708 A CN201310243708 A CN 201310243708A CN 103343881 A CN103343881 A CN 103343881A
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- 238000005516 engineering process Methods 0.000 title claims abstract description 23
- 238000011084 recovery Methods 0.000 title claims abstract description 18
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 196
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 98
- 238000001816 cooling Methods 0.000 claims abstract description 45
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 32
- 230000006835 compression Effects 0.000 claims abstract description 9
- 238000007906 compression Methods 0.000 claims abstract description 9
- 230000008676 import Effects 0.000 claims description 69
- 238000004519 manufacturing process Methods 0.000 claims description 3
- 239000007789 gas Substances 0.000 abstract description 14
- 238000000034 method Methods 0.000 abstract description 11
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 2
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 230000003247 decreasing effect Effects 0.000 abstract 1
- 239000003949 liquefied natural gas Substances 0.000 description 36
- 238000009833 condensation Methods 0.000 description 3
- 230000005494 condensation Effects 0.000 description 3
- 238000013461 design Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 238000012360 testing method Methods 0.000 description 2
- 238000011282 treatment Methods 0.000 description 2
- 229910000831 Steel Inorganic materials 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 235000019628 coolness Nutrition 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 239000002360 explosive Substances 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000001105 regulatory effect Effects 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 238000010792 warming Methods 0.000 description 1
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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
- F25J1/0002—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
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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
- F25J1/003—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
- F25J1/005—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 expansion of a gaseous refrigerant stream with extraction of work
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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
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
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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
- F25J1/0203—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—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 single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
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- 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
The invention discloses a technology of BOG recovery and a device of the technology of the BOG recovery. According to the technology of the BOG recovery, nitrogen from a nitrogen storage tank is compressed, and high-pressure nitrogen is obtained and enters a BOG recovery system; in the BOG recovery system, water cooling is performed on the nitrogen, then heat exchanging is performed on the nitrogen, low-temperature and high-pressure nitrogen is obtained and expanded to be in a normal-pressure state, temperature is further decreased, cooling capacity contained in the nitrogen is supplied to BOG from an LNG storage tank so that the BOG can be liquefied, and after the temperature of the nitrogen in the BOG recovery system goes up again to the temperature of the nitrogen storage tank, the nitrogen returns to the nitrogen storage tank. Through the method, using of an imported BOG compressor and compression of flammable and combustible hydrocarbon gas are omitted, the stable nitrogen serves as a cold carrier medium, and the BOG recovery is achieved through a common compressor and a common expanded machine in the market. The technology of the BOG recovery and the device are convenient to control, safe, simple in technological process and small in equipment investment, and have good industrialized popularization and application prospects.
Description
Technical field
The present invention relates to the LNG(LNG Liquefied natural gas) storage and transportation technology field, be specifically related to a kind of recovery BOG(flash steam) technology and device thereof.
Background technique
The LNG storage tank is the nucleus equipment of LNG receiving terminal, belongs to normal pressure, low temperature large-scale storage tank, and partial L NG receiving station also is provided with LNG tank car loading station.Because the LNG storage temperature is-162 ℃, external heat constantly sees through tank body material, attached pipe fitting etc. and passes to tank inside, part mechanical energy was converted into heat energy when Under Water Pumps moved in the LNG jar, in addition, outside LNG sends into the volume replacement that (as the discharging of LNG ship time) produces from tank deck, make the LNG evaporation form BOG(boil off gas), general steam output is the 0.05%(quality).In order to guarantee tank inner pressure in the scope that design allows, when the jar internal pressure rises to certain value, need by the boil-off gas processing system part BOG in the jar to be got rid of.
The method of treatments B OG mainly contains at present:
(1) storage tank BOG gas is returned the LNG ship, fill up the vacuum that cabin jar discharging produces; This method is succinct, efficient, but only just can balance a part of BOG gas when the discharging of LNG ship, and all the other situations are next can't be used.
(2) send torch or row's atmosphere; This method is applicable to the emergency safety measure, and is obviously unreasonable on economy, environmental issue.
(3) directly export technology, after namely the BOG gas of LNG storage tank directly is pressurized to the required pressure of gas ductwork by compressor, enter outer defeated pipe network.
(4) condensation process again, namely the BOG gas of LNG storage tank is by compressor pressurizes, and the Under Water Pumps in the storage tank is sent the LNG of uniform pressure, both direct heat transfers in after-condenser by a certain percentage.LNG cold excessively after the pressurization utilizes " showing cold " with most of BOG condensation of gas, again through the pressurization of second level pump, sends into high pressure pipe network after the vaporizer gasification.
General directly the output technology and condensation process treatments B OG again of adopting of LNG receiving station.Two kinds of technologies, BOG compressor all are the key equipments that boil-off gas is handled, and generally adopt low temperature not have oily reciprocating compressor.At present, domestic compressor is made the mature experience that factory does not still have design, makes the nothing oil reciprocating compressor that may operate under (rock gas) inlet temperature-160 ℃ low temperature, ripe to design, manufacturing, test and the check progression of compressor abroad, the BOG compressor manufacturer of usefulness has Burkhard (Burkhardt compression) company of Switzerland, the Ishikawa island of Japan to broadcast mill towards Dresser-Rand (Dresser-Rand) company of Industrial Co., Ltd (HI), Japanese kobe steel (KOBESTEEL) and the U.S..
The BOG compressor is equipment usefulness not generally, occurs under the chance failure situation at the BOG compressor, needs maintenance for a long time, the flare system that excess steam is then discharged.Domesticly all need introduce external BOG compressor apparatus, and in the operation corresponding technology of shortcoming and the experience of test, check, limit economy and operability that BOG reclaims.
Summary of the invention
The object of the invention is to overcome the prior art defective, solve the problem that BOG reclaims needs to introduce external BOG compressor, adopt reciprocating expansion engine commonly used and compressor to realize BOG recoverys of liquefying again, namely proposing provides cold to BOG with low temperature nitrogen for carrying a cold medium, makes its liquefaction recovery.Do not need to use the BOG compressor, by the connecting shaft running of nitrogen compressor and decompressor, replenish external power drive compression machine simultaneously and obtain high pressure nitrogen, obtain low temperature nitrogen after the expansion, make its liquefaction for the BOG cooling again, nitrogen circulation is used.Native system is safe and reliable, and is simple in structure, with low cost.
The object of the invention is achieved through the following technical solutions:
A kind of technology that reclaims BOG, the nitrogen compression that it will come from nitrogen storage tank obtains high pressure nitrogen, and high pressure nitrogen enters the BOG reclaiming system; In the BOG reclaiming system, high pressure nitrogen obtains cryogenic high pressure nitrogen through the water-cooled heat exchange; Cryogenic high pressure nitrogen is expanded to atmospheric pressure state again, temperature further reduces, the cold that this part nitrogen contains is supplied with the BOG that comes from the LNG storage tank, make BOG liquefaction, nitrogen is back to nitrogen storage tank behind the temperature recovery in the BOG reclaiming system, the nitrogen that the is back to nitrogen storage tank aforesaid manufacturing process that circulates again.
The technology of above-mentioned recovery BOG further may further comprise the steps:
(1) first control valve, second control valve, the 3rd control valve, the 5th control valve are opened, and all the other control valves are closed; 0.1 ~ 0.2MPa, 15 ~ 25 ℃ nitrogen are exported by nitrogen storage tank, enter first compressor, are compressed to 0.3～0.8MPa, temperature becomes 120～290 ℃, enter first water cooling heat exchanger then, with 10 ~ 15 ℃, the water heat exchange of 0.1 ~ 0.2MPa, nitrogen temperature is reduced to 20～30 ℃;
(2) 20～30 ℃ nitrogen is divided into two strands, one second control valve of flowing through, one the 3rd control valve of flowing through.The nitrogen of the 3rd control valve of wherein flowing through is introduced into the second compression increasing temperature and pressure, enter the cooling of second water cooling heat exchanger then, expand through first decompressor, temperature is reduced to-120～-130 ℃, pressure is reduced to 0.1 ~ 0.2MPa, flow to the cold logistics import of first heat exchanger;
(3) flow through 20～30 ℃ of nitrogen of second control valve through first heat exchanger heat exchange cooling back from the hot logistics outlet outflow of first heat exchanger, expand through second decompressor again and lower the temperature, pressure is reduced to 0.1 ~ 0.2MPa, flow to the cold logistics import of first heat exchanger through the 5th control valve, the nitrogen that comes out with first decompressor is combined into one, enter the first heat exchanger heat exchange, temperature is increased to 15～25 ℃ and returns nitrogen storage tank;
(4) when from 20～30 ℃ nitrogen of second control valve after first heat exchanger heat exchange cooling, when temperature remains on-140～-150 ℃, close the 3rd control valve and the 5th control valve, open the 4th control valve and the 6th control valve, regulate first control valve, the nitrogen flow of second control valve of flowing through in the nitrogen flow that nitrogen storage tank 1 is flowed out in control and the step is identical;
(5) described-140～-150 ℃ nitrogen expands cooling for-180 ~-195 ℃ through second decompressor, in second heat exchanger cold being passed to the BOG that comes from the LNG storage tank reclaims its liquefaction, nitrogen temperature gos up to-150 ~-170 ℃, be back to the cold logistics import of first heat exchanger, in first heat exchanger, will be cooled to-140～-150 ℃ from the nitrogen of second control valve, self temperature is increased to 15～25 ℃ and returns nitrogen storage tank, temperature is reduced to 20～30 ℃ behind first compressor and first water cooling heat exchanger again, reduce to-140～-150 ℃ through first heat exchange temperature, enter second decompressor and expand cooling for-180 ~-195 ℃, in second heat exchanger cold is passed to the BOG that comes from the LNG storage tank its liquefaction is reclaimed, BOG is continuously reclaimed in circulation according to this.
In this technological process, compressor and the running of decompressor connecting shaft, i.e. first compressor and second decompressor connecting shaft running, second compressor and the running of the first decompressor connecting shaft, expansion work is directly supplied with compressor, compressor connects power supply simultaneously, replenishes the electric power that needs by externally fed.
The inventive method, simple to operate, equipment is common expansion, compression and heat transmission equipment, and is all very common on the Domestic market.
Implement the device of described technology, comprise nitrogen storage tank, first compressor, second compressor, first decompressor, second decompressor, LNG storage tank, first water cooling heat exchanger, second water cooling heat exchanger, first heat exchanger, second heat exchanger, pump, first flow meter, second flowmeter, the 3rd flowmeter, first control valve, second control valve, the 3rd control valve, the 4th control valve, the 5th control valve, the 6th control valve; Described nitrogen storage tank is connected with the first flow meter by first control valve with first compressor, the outlet of first compressor is connected with the hot logistics import of first water cooling heat exchanger, the hot logistics outlet bifurcation of first water cooling heat exchanger, one is connected with the import of second compressor by the 3rd control valve, and another passes through second control valve, and hot logistics import is connected with second flowmeter, first water cooling heat exchanger; The outlet of second compressor is connected with the hot logistics import of second water cooling heat exchanger, the outlet of hot logistics is connected with the import of first decompressor, the outlet of first decompressor is connected with the cold logistics import of first heat exchanger, the cold logistics outlet of first heat exchanger is connected with the import of nitrogen storage tank, the outlet of hot logistics is connected with the import of second decompressor, the outlet of second decompressor is told two, one is passed through the 5th control valve and is connected with the cold logistics import of first heat exchanger, another is connected by the 6th control valve with the cold logistics import of second heat exchanger, the cold logistics outlet of second heat exchanger is connected with the cold logistics import of first heat exchanger, the outlet of LNG storage tank is connected with the hot logistics import of second heat exchanger with the 3rd flowmeter by the 4th control valve, hot logistics outlet then is connected with the import of pump, and delivery side of pump is connected with the import of LNG storage tank.
The cold logistics import of described first heat exchanger is connected by hot insulated line with the outlet of first decompressor; Hot logistics outlet is connected by hot insulated line with the import of second decompressor;
The outlet of described second decompressor is connected by hot insulated line with the cold logistics import of second heat exchanger;
The outlet of described LNG storage tank is connected by hot insulated line with the hot logistics import of second heat exchanger;
The hot logistics outlet of described second heat exchanger all is connected with hot insulated line with the import of LNG storage tank with the import of pump and delivery side of pump;
Compared with prior art, the present invention has the following advantages:
1, equipment cost is low, invests little: reclaiming BOG at present all needs import BOG compressor, and common compressor and decompressor cooling on the market adopted in this invention, and BOG liquefaction is reclaimed;
2, easy to operate, safety: original BOG reclaims technology, all need to utilize BOG compressor compresses BOG, and hydrocarbon gas belongs to flammable explosive gas, there is potential safety hazard, this invented technology adopts nitrogen to be a year cold medium, and is security and stability gas, and compression and expansion can not bring danger;
3, stability is high: technological process is simple, after the start, and the nitrogen circulation cooling, flowmeter and control valve are stable.
Description of drawings
Fig. 1 is recovery BOG technology of the present invention and device thereof.
Embodiment
Below in conjunction with accompanying drawing and example enforcement of the present invention is described further, but enforcement of the present invention and protection are not limited thereto.
The device of this example comprises nitrogen storage tank 1, first compressor 4, second compressor 8, first decompressor 10, second decompressor 13, LNG storage tank 16, first water cooling heat exchanger 5, second water cooling heat exchanger 9, first heat exchanger 12, second heat exchanger 14, pump 15, first flow meter 3, second flowmeter 11, the 3rd flowmeter 18, first control valve 2, second control valve 6, the 3rd control valve 7, the 4th control valve 17, the 5th control valve 19, the 6th control valve 20; Described nitrogen storage tank 1 is connected with first flow meter 3 by first control valve 2 with first compressor 4, the outlet of first compressor 4 is connected with the hot logistics import of first water cooling heat exchanger 5, the hot logistics outlet bifurcation of first water cooling heat exchanger 5, one is connected with the import of second compressor 8 by the 3rd control valve 7, and another passes through second control valve 6, and 5 hot logistics imports are connected with second flowmeter, 11 first water cooling heat exchangers; The outlet of second compressor 8 is connected with the hot logistics import of second water cooling heat exchanger 9, the outlet of hot logistics is connected with the import of first decompressor 10, the outlet of first decompressor 10 is connected with the cold logistics import of first heat exchanger 12, the 12 cold logistics outlets of first heat exchanger are connected with the import of nitrogen storage tank 1, the outlet of hot logistics is connected with the import of second decompressor 13, the outlet of second decompressor 13 is told two, one is passed through the 5th control valve 19 and is connected with the 12 cold logistics imports of first heat exchanger, another is connected by the 6th control valve 20 with the cold logistics import of second heat exchanger 14, the cold logistics outlet of second heat exchanger 14 is connected with the 12 cold logistics imports of first heat exchanger, the outlet of LNG storage tank 16 is connected with the hot logistics import of second heat exchanger 14 with the 3rd flowmeter 18 by the 4th control valve 17, hot logistics outlet then is connected with the import of pump 15, and the outlet of pump 15 is connected with the import of LNG storage tank 16.
The cold logistics import of described first heat exchanger 12 is connected by hot insulated line with the outlet of first decompressor 10; Hot logistics outlet is connected by hot insulated line with the import of second decompressor 13;
The outlet of described second decompressor 13 is connected by hot insulated line with the cold logistics import of second heat exchanger 14;
The outlet of described LNG storage tank 16 is connected by hot insulated line with the hot logistics import of second heat exchanger 14;
The hot logistics outlet of described second heat exchanger 14 all is connected with hot insulated line with the import of LNG storage tank 16 with the outlet of the import of pump 15 and pump 15.
Utilize said apparatus to reclaim the technology of BOG, may further comprise the steps:
(1) first control valve 2, second control valve 6, the 3rd control valve 7, the 5th control valve 19 are opened, and all the other control valves are closed, 0.12MPa, 18 ℃, 1370kg/h(1096Nm
3/ h) nitrogen enters in first compressor 4 through first control valve 2, is compressed to 0.8MPa, and temperature is increased to 277 ℃, enter in first water cooling heat exchanger 5, through 10 ℃, 0.2MPa be water-cooled to 22 ℃, pressure still is 0.8MPa,
(2) 22 ℃ nitrogen is divided into two strands, and one is 730kg/h(584Nm
3/ h) second control valve 6 of flowing through, another strand is 640kg/h(512Nm
3/ h) the 3rd control valve 7 of flowing through;
640kg/h(512Nm
3/ h) nitrogen earlier is compressed to 3.2MPa through second compressor 8, enter second water cooling heat exchanger, 9 water-cooleds after, expand through first decompressor 10, pressure is reduced to 0.13MPa, temperature is reduced to-122 ℃, flow to the cold logistics import of first heat exchanger 12.
(3) 22 ℃, 730kg/h nitrogen enter in first heat exchanger 12, hot logistics outlet from first heat exchanger 12 after the heat exchange cooling is flowed out, be expanded to 0.13MPa through second decompressor 13 again, flow to the cold logistics import of first heat exchanger 12 by the 5th control valve 19, the nitrogen that comes out with first decompressor 10 is combined into one, enter 12 heat exchange of first heat exchanger, temperature is increased to 18 ℃ and returns nitrogen storage tank 1.
(4) when system stable namely from 22 ℃ nitrogen of second control valve 6 after first heat exchanger, 12 heat exchange cooling, when temperature reaches-145 ℃, close the 3rd control valve 7, the 5th control valve 19, regulate first control valve 2, the nitrogen flow that nitrogen storage tank 1 is flowed out in control is 730kg/h(584Nm
3/ h), open the 4th control valve 17, the 6th control valve 20, regulating the 4th control valve 17, to use the BOG flow of LNG storage tank 16 be 50kg/h;
(5) regulate after first control valve 2 and the 4th control valve 17,-145 ℃ nitrogen is reduced to-190 ℃ through second decompressor, 13 temperature, pressure is reduced to 0.13MPa, enter in second heat exchanger 14, with the BOG heat exchange that comes from LNG storage tank 16, make it be liquefied as LNG and be back in the LNG storage tank 16 by pump 15, nitrogen then is warming up to-155 ℃, return in first heat exchanger 12, with 22 ℃, 0.8MPa, the 730kg/h(584Nm of cold supply from second control valve 6
3/ h) nitrogen, make this strand nitrogen temperature reduce to-145 ℃, return in the nitrogen storage tank 1 behind self temperature recovery to 18 ℃, temperature becomes 22 ℃ behind first compressor 4 and first water cooling heat exchanger 5 again, reduce to-145 ℃ through first heat exchanger, 12 temperature, enter the 13 expansion coolings of second decompressor and be-190 ℃, in second heat exchanger 14, cold is passed to the BOG that comes from LNG storage tank 16 its liquefaction is reclaimed, circulate according to this and continuously reclaim BOG.
Above parameter is the value of ideal or optimum state, and because of affected by environment, those skilled in the art can do corresponding adjustment during practical operation, to reach the purpose that reclaims BOG.
Claims (6)
1. a technology that reclaims BOG is characterized in that obtaining high pressure nitrogen with coming from the nitrogen compression of nitrogen storage tank, and high pressure nitrogen enters the BOG reclaiming system; In the BOG reclaiming system, high pressure nitrogen obtains cryogenic high pressure nitrogen through the water-cooled heat exchange; Cryogenic high pressure nitrogen is expanded to atmospheric pressure state again, temperature further reduces, the cold that this part nitrogen contains is supplied with the BOG that comes from the LNG storage tank, make BOG liquefaction, nitrogen is back to nitrogen storage tank behind the temperature recovery in the BOG reclaiming system, the nitrogen that the is back to nitrogen storage tank aforesaid manufacturing process that circulates again.
2. a kind of technology that reclaims BOG according to claim 1 is characterized in that may further comprise the steps:
(1) first control valve (2), second control valve (6), the 3rd control valve (7), the 5th control valve (19) are opened, and all the other control valves are closed; 0.1 ~ 0.2MPa, 15 ~ 25 ℃ nitrogen are exported by nitrogen storage tank (1), enter first compressor (4), be compressed to 0.3～0.8MPa, temperature becomes 120～290 ℃, enter first water cooling heat exchanger (5) then, with 10 ~ 15 ℃, the water heat exchange of 0.1 ~ 0.2MPa, nitrogen temperature is reduced to 20～30 ℃;
(2) 20～30 ℃ nitrogen is divided into two strands, one second control valve (6) of flowing through, and one the 3rd control valve (7) of flowing through,
The nitrogen of the 3rd control valve (7) of wherein flowing through is introduced into second compression (8) increasing temperature and pressure, enter second water cooling heat exchanger (9) cooling then, expand through first decompressor (10) again, temperature is reduced to-120～-130 ℃, pressure is reduced to 0.1 ~ 0.2MPa, flow to the cold logistics import of first heat exchanger (12);
(3) flow through 20～30 ℃ of nitrogen of second control valve (6) through first heat exchanger (12) heat exchange cooling back from the hot logistics outlet outflow of first heat exchanger (12), expand through second decompressor (13) again and lower the temperature, pressure is reduced to 0.1 ~ 0.2MPa, flow to the cold logistics import of first heat exchanger (12) through the 5th control valve (19), the nitrogen that comes out with first decompressor (10) is combined into one, enter first heat exchanger (12) heat exchange, temperature is increased to 15～25 ℃ and returns nitrogen storage tank (1);
(4) when from 20～30 ℃ nitrogen of second control valve (6) after first heat exchanger (12) heat exchange cooling, when temperature remains on-140～-150 ℃, close the 3rd control valve (7) and the 5th control valve (19), open the 4th control valve (17) and the 6th control valve (20), regulate first control valve (2), the nitrogen flow of second control valve (6) of flowing through in the nitrogen flow that nitrogen storage tank 1 is flowed out in control and the step (2) is identical;
(5) described-140～-150 ℃ nitrogen expands cooling for-180 ~-195 ℃ through second decompressor (13), in second heat exchanger (14) cold being passed to the BOG that comes from LNG storage tank (16) reclaims its liquefaction, nitrogen temperature gos up to-150 ~-170 ℃, be back to the cold logistics import of first heat exchanger (12), in first heat exchanger (12), will be cooled to-140～-150 ℃ from the nitrogen of second control valve (6), self temperature is increased to 15～25 ℃ and returns nitrogen storage tank (1), temperature is reduced to 20～30 ℃ behind first compressor (4) and first water cooling heat exchanger (5) again, reduce to-140～-150 ℃ through first heat exchanger (12) temperature, enter second decompressor (13) and expand cooling for-180 ~-195 ℃, in second heat exchanger (14) cold is passed to the BOG that comes from LNG storage tank (16) its liquefaction is reclaimed, BOG is continuously reclaimed in circulation according to this.
3. a kind of technology that reclaims BOG according to claim 2, it is characterized in that for described first compressor (4) and the running of second decompressor (13) connecting shaft, second compressor (8) and the running of first decompressor (10) connecting shaft, expansion work is directly supplied with compressor, compressor connects power supply simultaneously, replenishes the electric power that needs by externally fed.
4. realize the device of the technology of each described recovery BOG of claim 1 ~ 3, it is characterized in that comprising nitrogen storage tank (1), first compressor (4), second compressor (8), first decompressor (10), second decompressor (13), LNG storage tank (16), first water cooling heat exchanger (5), second water cooling heat exchanger (9), first heat exchanger (12), second heat exchanger (14), pump (15), first flow meter (3), second flowmeter (11), the 3rd flowmeter (18), first control valve (2), second control valve (6), the 3rd control valve (7), the 4th control valve (17), the 5th control valve (19), the 6th control valve (20); Described nitrogen storage tank (1) is connected with first flow meter (3) by first control valve (2) with first compressor (4), the outlet of first compressor (4) is connected with the hot logistics import of first water cooling heat exchanger (5), the hot logistics outlet bifurcation of first water cooling heat exchanger (5), one is connected with the import of second compressor (8) by the 3rd control valve (7), and another passes through second control valve (6), and hot logistics import is connected with second flowmeter (11) first water cooling heat exchangers (5); The outlet of second compressor (8) is connected with the hot logistics import of second water cooling heat exchanger (9), the outlet of hot logistics is connected with the import of first decompressor (10), the outlet of first decompressor (10) is connected with the cold logistics import of first heat exchanger (12), the cold logistics outlet of first heat exchanger (12) is connected with the import of nitrogen storage tank (1), the outlet of hot logistics is connected with the import of second decompressor (13), the outlet of second decompressor (13) is told two, one is passed through the 5th control valve (19) and is connected with the cold logistics import of first heat exchanger (12), another is connected by the 6th control valve (20) with the cold logistics import of second heat exchanger (14), the cold logistics outlet of second heat exchanger (14) is connected with the cold logistics import of first heat exchanger (12), the outlet of LNG storage tank (16) is connected with the hot logistics import of second heat exchanger (14) with the 3rd flowmeter (18) by the 4th control valve (17), hot logistics outlet then is connected with the import of pump (15), and the outlet of pump (15) is connected with the import of LNG storage tank (16).
5. device according to claim 4 is characterized in that, the cold logistics import of described first heat exchanger (12) is connected by hot insulated line with the outlet of first decompressor (10); Hot logistics outlet is connected by hot insulated line with the import of second decompressor (13); The outlet of second decompressor (13) is connected by hot insulated line with the cold logistics import of second heat exchanger (14); The outlet of LNG storage tank (16) is connected by hot insulated line with the hot logistics import of second heat exchanger (14); The hot logistics outlet of second heat exchanger (14) all is connected with hot insulated line with the import of LNG storage tank (16) with the outlet of the import of pump (15) and pump (15).
6. device according to claim 4 is characterized in that, described compressor adopts reciprocal compressor, and described decompressor adopts reciprocating expansion engine.
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| CN104141881A (en) * | 2014-07-18 | 2014-11-12 | 江汉石油钻头股份有限公司 | Heat transfer system utilizing normal temperature compressor to compress cryogenic medium |
| CN104482395A (en) * | 2014-11-05 | 2015-04-01 | 中海福建天然气有限责任公司 | Method for utilizing LNG (Liquefied Natural Gas) cold energy to recover BOG (Boil Off Gas) generated during entrucking of tank car |
| CN104482396A (en) * | 2014-11-11 | 2015-04-01 | 南京工业大学 | Novel high-efficiency BOG recovery system with cold storage function |
| CN105333693A (en) * | 2015-11-17 | 2016-02-17 | 江苏航天惠利特环保科技有限公司 | Efficient and energy-saving BOG (boil-off gas) recycling device |
| CN105674054A (en) * | 2014-11-17 | 2016-06-15 | 罗纳德·格兰特·肖莫迪 | Waste gas treatment and transportation for conserving resources and reducing emission |
| CN106051459A (en) * | 2016-07-14 | 2016-10-26 | 青岛华控能源科技有限公司 | Two-stage pressure boosting recovering and energy saving system used in tire nitrogen curing |
| CN108679444A (en) * | 2018-06-06 | 2018-10-19 | 张家港艾普能源装备有限公司 | LNG storage tank is utilizing device |
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| CN104141881A (en) * | 2014-07-18 | 2014-11-12 | 江汉石油钻头股份有限公司 | Heat transfer system utilizing normal temperature compressor to compress cryogenic medium |
| CN104482395A (en) * | 2014-11-05 | 2015-04-01 | 中海福建天然气有限责任公司 | Method for utilizing LNG (Liquefied Natural Gas) cold energy to recover BOG (Boil Off Gas) generated during entrucking of tank car |
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| CN105674054A (en) * | 2014-11-17 | 2016-06-15 | 罗纳德·格兰特·肖莫迪 | Waste gas treatment and transportation for conserving resources and reducing emission |
| CN105333693A (en) * | 2015-11-17 | 2016-02-17 | 江苏航天惠利特环保科技有限公司 | Efficient and energy-saving BOG (boil-off gas) recycling device |
| CN106051459A (en) * | 2016-07-14 | 2016-10-26 | 青岛华控能源科技有限公司 | Two-stage pressure boosting recovering and energy saving system used in tire nitrogen curing |
| CN108679444A (en) * | 2018-06-06 | 2018-10-19 | 张家港艾普能源装备有限公司 | LNG storage tank is utilizing device |
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