CN103343881B - A kind of technique and device thereof reclaiming BOG - Google Patents
A kind of technique and device thereof reclaiming BOG Download PDFInfo
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- CN103343881B CN103343881B CN201310243708.5A CN201310243708A CN103343881B CN 103343881 B CN103343881 B CN 103343881B CN 201310243708 A CN201310243708 A CN 201310243708A CN 103343881 B CN103343881 B CN 103343881B
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- 238000000034 method Methods 0.000 title claims abstract description 28
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims abstract description 192
- 229910052757 nitrogen Inorganic materials 0.000 claims abstract description 96
- 230000008676 import Effects 0.000 claims abstract description 70
- 238000011084 recovery Methods 0.000 claims abstract description 15
- 230000006835 compression Effects 0.000 claims abstract description 9
- 238000007906 compression Methods 0.000 claims abstract description 9
- 238000001816 cooling Methods 0.000 claims description 44
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 31
- 238000004519 manufacturing process Methods 0.000 claims description 4
- 239000007789 gas Substances 0.000 abstract description 15
- 239000004215 Carbon black (E152) Substances 0.000 abstract description 2
- 239000002360 explosive Substances 0.000 abstract description 2
- 229930195733 hydrocarbon Natural products 0.000 abstract description 2
- 150000002430 hydrocarbons Chemical class 0.000 abstract description 2
- 239000003949 liquefied natural gas Substances 0.000 description 37
- 238000013461 design Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000001276 controlling effect Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 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
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000007547 defect Effects 0.000 description 1
- 230000007613 environmental effect Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 238000007689 inspection Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 239000010959 steel Substances 0.000 description 1
- 239000013589 supplement Substances 0.000 description 1
- 239000006200 vaporizer Substances 0.000 description 1
- 238000010792 warming Methods 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
- F25J1/0002—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
- F25J1/0047—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
Abstract
The invention discloses a kind of technique and the device thereof that reclaim BOG.The present invention will come from the nitrogen compression of nitrogen storage tank, obtain high pressure nitrogen, enter BOG reclaiming system; In BOG reclaiming system, nitrogen water-cooled, then heat exchange obtains cryogenic high pressure nitrogen, reflation is to atmospheric pressure state, temperature reduces further, and the cold supply of being contained by this part nitrogen comes from the BOG of LNG storage tank, makes it liquefy, nitrogen after temperature recovery to nitrogen storage tank temperature, is back to nitrogen storage tank in BOG reclaiming system.The method eliminates the use of import BOG compressor and the compression to inflammable and explosive hydrocarbon gas, with stability gas nitrogen for refrigerating medium, the recovery of BOG is realized by compressor common on market and decompressor, control convenient, safety, technological process is simple, equipment investment is little, has good commercial introduction application prospect.
Description
Technical field
The present invention relates to LNG(LNG Liquefied natural gas) store and technical field of transportation, be specifically related to a kind of reclaim BOG(flash steam) technique and device.
Background technique
LNG storage tank is the nucleus equipment of LNG receiving terminal, belongs to normal pressure, low temperature large-scale storage tank, and part LNG receiving station is also provided with LNG tank car loading station.Because LNG storage temperature is-162 DEG C, external heat constantly passes to tank inside through tank body material, attached pipe fitting etc., when in LNG tank, Under Water Pumps runs, some mechanical can be converted into heat energy, in addition, the volume replacement that outside LNG produces from tank deck feeding (during as LNG ship discharging), LNG is evaporated and forms BOG(boil off gas), general steam output is 0.05%(quality).In order to ensure that tank inner pressure is in the scope that design allows, when tank internal pressure rises to certain value, by boil-off gas processing system, part BOG in tank need be got rid of.
The method of current treatments B OG mainly contains:
(1) storage tank BOG gas is returned LNG ship, fill up the vacuum that cabin tank discharging produces; The method is succinct, efficient, but only just can balance a part of BOG gas when LNG ship discharging, then cannot use in all the other situations.
(2) torch or row's air is sent; The method is applicable to emergency safety measure, obviously unreasonable in economy, environmental issue.
(3) directly export technique, namely the BOG gas of LNG storage tank is by after pressure needed for compressor direct weighting to gas ductwork, enters outer defeated pipe network.
(4) recondensation process, namely the BOG gas of LNG storage tank is by compressor pressurizes, and the Under Water Pumps in storage tank sends the LNG of uniform pressure, both direct heat transfers in after-condenser by a certain percentage.LNG excessively cold after pressurization utilizes " aobvious cold " by most of BOG condensation of gas, then through the pressurization of second level pump, after vaporizer gasification, sends into high pressure pipe network.
LNG receiving station generally adopts and directly exports technique and recondensation process treatments B OG.Two kinds of techniques, BOG compressor is all the key equipment of boil-off gas process, and the general low temperature that adopts is without oily reciprocating compressor.At present, domestic Compressor Manufacturing factory there is no design, manufactures the mature experience without oily reciprocating compressor that may operate under (rock gas) inlet temperature-160 DEG C of low temperature, ripe to the design of compressor, manufacture, test load-efficiency progression abroad, there is Dresser-Rand (Dresser-Rand) company of Burkhard (Burkhardt compression) company of Switzerland, the Ishikawa Dao Bomochong Industrial Co., Ltd (HI) of Japan, Japanese kobe steel (KOBESTEEL) and the U.S. in BOG compressor manufacturer.
The general not equipment use of BOG compressor, under chance failure situation appears in BOG compressor, needs to keep in repair for a long time, the flare system that excess steam is then discharged.Domesticly all need Introduced From Abroad BOG compressor apparatus, and be short of corresponding technology and experience in the operation of test, inspection, limit economy and operability that BOG reclaims.
Summary of the invention
The object of the invention is to overcome prior art defect, solve BOG and reclaim the problem needing Introduced From Abroad BOG compressor, adopt conventional reciprocating expansion engine and compressor to realize BOG to liquefy again recovery, namely propose with low temperature nitrogen to be that refrigerating medium provides cold to BOG, make its recovery of liquefying.Do not need to use BOG compressor, operated by the connecting shaft of nitrogen compressor and decompressor, supplement external power simultaneously and drive compressor to obtain high pressure nitrogen, obtain low temperature nitrogen after expansion, then make it liquefy to BOG cooling, nitrogen circulation uses.Native system is safe and reliable, and structure is simple, with low cost.
The object of the invention is achieved through the following technical solutions:
Reclaim a technique of BOG, it will come from the nitrogen compression of nitrogen storage tank, and obtain high pressure nitrogen, high pressure nitrogen enters BOG reclaiming system; In BOG reclaiming system, high pressure nitrogen, through water-cooled heat exchange, obtains cryogenic high pressure nitrogen; Cryogenic high pressure nitrogen reflation is to atmospheric pressure state, temperature reduces further, the cold supply of being contained by this part nitrogen comes from the BOG of LNG storage tank, BOG is liquefied, nitrogen is back to nitrogen storage tank after temperature recovery in BOG reclaiming system, and the nitrogen being back to nitrogen storage tank circulates aforesaid manufacturing process again.
The technique of above-mentioned recovery BOG, further comprising the steps:
(1) first control valve, the 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, the nitrogen of 15 ~ 25 DEG C are exported by nitrogen storage tank, enter the first compressor, are compressed to 0.3 ~ 0.8MPa, temperature becomes 120 ~ 290 DEG C, then enter the first water cooling heat exchanger, with 10 ~ 15 DEG C, the water heat exchange of 0.1 ~ 0.2MPa, nitrogen temperature reduces to 20 ~ 30 DEG C;
The nitrogen of (2) 20 ~ 30 DEG C is divided into two strands, and one flows through the second control valve, and one flows through the 3rd control valve.The nitrogen wherein flowing through the 3rd control valve is introduced into the second compression increasing temperature and pressure, then enter the second water cooling heat exchanger cooling, then through the first expander, temperature reduces to-120 ~-130 DEG C, pressure reduces to 0.1 ~ 0.2MPa, flow to the cold logistics import of First Heat Exchanger;
(3) the hot stream outlet of 20 ~ 30 DEG C of nitrogen from First Heat Exchanger after First Heat Exchanger heat exchange cooling flowing through the second control valve flows out, again through the second expander cooling, pressure reduces to 0.1 ~ 0.2MPa, the cold logistics import of First Heat Exchanger is flow to through the 5th control valve, one is combined into the first decompressor nitrogen out, enter First Heat Exchanger heat exchange, temperature is increased to 15 ~ 25 DEG C and returns nitrogen storage tank;
(4) when the nitrogen of 20 ~ 30 DEG C from the second control valve is after First Heat Exchanger heat exchange cooling, when temperature remains on-140 ~-150 DEG C, close the 3rd control valve and the 5th control valve, open the 4th control valve and the 6th control valve, regulate the first control valve, the nitrogen flow controlling to flow out nitrogen storage tank 1 is identical with the nitrogen flow flowing through the second control valve in step;
(5) nitrogen of described-140 ~-150 DEG C is-180 ~-195 DEG C through the second expander cooling, in the second heat exchanger cold is passed to the BOG coming from LNG storage tank and make its recovery of liquefying, nitrogen temperature gos up to-150 ~-170 DEG C, be back to the cold logistics import of First Heat Exchanger, in First Heat Exchanger, the nitrogen from the second control valve is cooled to-140 ~-150 DEG C, own temperature is increased to 15 ~ 25 DEG C and returns nitrogen storage tank, after the first compressor and the first water cooling heat exchanger, temperature reduces to 20 ~ 30 DEG C again,-140 ~-150 DEG C are reduced to through First Heat Exchanger temperature, enter the second expander cooling for-180 ~-195 DEG C, in the second heat exchanger cold is passed to the BOG coming from LNG storage tank and make its recovery of liquefying, circulate according to this and continuously reclaim BOG.
In this technological process, compressor and decompressor connecting shaft operate, i.e. the first compressor and the running of the second decompressor connecting shaft, the second compressor and the running of the first decompressor connecting shaft, and expansion work directly supplies compressor, compressor connects power supply simultaneously, is supplemented the electric power of needs by externally fed.
The inventive method, simple to operate, equipment is common expansion, compression and heat transmission equipment, all very common on Domestic market.
The device of the technique described in enforcement, comprises nitrogen storage tank, the first compressor, the second compressor, the first decompressor, the second decompressor, LNG storage tank, the first water cooling heat exchanger, the second water cooling heat exchanger, First Heat Exchanger, the second heat exchanger, pump, first-class gauge, second gauge, the 3rd flowmeter, the first control valve, the 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 by the first control valve and first-class gauge with the first compressor, the outlet of the first compressor is connected with the hot logistics import of the first water cooling heat exchanger, the hot stream outlet bifurcation of the first water cooling heat exchanger, one is connected with the import of the second compressor by the 3rd control valve, and another is connected with the hot logistics import of second gauge first water cooling heat exchanger by the second control valve, the outlet of the second compressor is connected with the hot logistics import of the second water cooling heat exchanger, the outlet of hot logistics is connected with the import of the first decompressor, the outlet of the first decompressor is connected with the cold logistics import of First Heat Exchanger, the cold stream 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 the second decompressor, the outlet of the second decompressor separates two, one is connected by the cold logistics import of the 5th control valve and First Heat Exchanger, another is connected by the 6th control valve with the cold logistics import of the second heat exchanger, the cold stream outlet of the 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 the second heat exchanger with the 3rd flowmeter by the 4th control valve, hot stream outlet is then connected with the import of pump, 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 the first decompressor; Hot stream outlet is connected by hot insulated line with the import of the second decompressor;
The outlet of described second decompressor is connected by hot insulated line with the cold logistics import of the second heat exchanger;
The outlet of described LNG storage tank is connected by hot insulated line with the hot logistics import of the second heat exchanger;
The hot stream outlet of described second heat exchanger is all 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 this invention adopts common compressor and decompressor cooling on market, BOG is liquefied and reclaims;
2, easy to operate, safety: original BOG recovery process, 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 refrigerating medium, and is security and stability gas, and compression and expansion all can not bring danger;
3, stability is high: technological process is simple, and after start, nitrogen circulation cooling, flowmeter and control valve are stablized.
Accompanying drawing explanation
Fig. 1 is recovery BOG technique 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-class gauge 3, second gauge 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 by the first control valve 2 and first-class gauge 3 with the first compressor 4, the outlet of the first compressor 4 is connected with the hot logistics import of the first water cooling heat exchanger 5, the hot stream outlet bifurcation of the first water cooling heat exchanger 5, one is connected by the import of the 3rd control valve 7 with the second compressor 8, and another is connected with the hot logistics import of second gauge 11 first water cooling heat exchanger 5 by the second control valve 6, the outlet of the second compressor 8 is connected with the hot logistics import of the second water cooling heat exchanger 9, the outlet of hot logistics is connected with the import of the first decompressor 10, the outlet of the first decompressor 10 is connected with the cold logistics import of First Heat Exchanger 12, the cold stream 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 the second decompressor 13, the outlet of the second decompressor 13 separates two, one is connected by the cold logistics import of the 5th control valve 19 and First Heat Exchanger 12, another is connected by the 6th control valve 20 with the cold logistics import of the second heat exchanger 14, the cold stream outlet of the 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 the second heat exchanger 14 with the 3rd flowmeter 18 by the 4th control valve 17, hot stream outlet is then connected with the import of pump 15, 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 the first decompressor 10; Hot stream outlet is connected by hot insulated line with the import of the second decompressor 13;
The outlet of described second decompressor 13 is connected by hot insulated line with the cold logistics import of the second heat exchanger 14;
The outlet of described LNG storage tank 16 is connected by hot insulated line with the hot logistics import of the second heat exchanger 14;
The described hot stream outlet of the second heat exchanger 14 is all connected with hot insulated line with the import of LNG storage tank 16 with the import of pump 15 and the outlet of pump 15.
Utilize said apparatus to reclaim the technique of BOG, comprise the following 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 DEG C, 1370kg/h(1096Nm
3/ h) nitrogen enter in the first compressor 4 through the first control valve 2, be compressed to 0.8MPa, temperature is increased to 277 DEG C, enters in the first water cooling heat exchanger 5, through 10 DEG C, 0.2MPa be water-cooled to 22 DEG C, pressure is still 0.8MPa,
The nitrogen of (2) 22 DEG C is divided into two strands, and one is 730kg/h(584Nm
3/ h) flow through the second control valve 6, another stock is 640kg/h(512Nm
3/ h) flow through the 3rd control valve 7;
640kg/h(512Nm
3/ h) nitrogen be first compressed to 3.2MPa through the second compressor 8, after entering the second water cooling heat exchanger 9 water-cooled, expand through the first decompressor 10, pressure reduces to 0.13MPa, and temperature reduces to-122 DEG C, flow to the cold logistics import of First Heat Exchanger 12.
(3) 22 DEG C, 730kg/h nitrogen enters in First Heat Exchanger 12, hot stream outlet from First Heat Exchanger 12 after heat exchange cooling flows out, 0.13MPa is expanded to again through the second decompressor 13, the cold logistics import of First Heat Exchanger 12 is flow to by the 5th control valve 19, one is combined into the first decompressor 10 nitrogen out, enter First Heat Exchanger 12 heat exchange, temperature is increased to 18 DEG C and returns nitrogen storage tank 1.
(4) when system run all right namely from the second control valve 6 the nitrogen of 22 DEG C through First Heat Exchanger 12 heat exchange cooling after, when temperature reaches-145 DEG C, close the 3rd control valve 7, the 5th control valve 19, regulate the first control valve 2, the nitrogen flow controlling to flow out nitrogen storage tank 1 is 730kg/h(584Nm
3/ h), open the 4th control valve 17, the 6th control valve 20, the BOG flow regulating the 4th control valve 17 to use LNG storage tank 16 is 50kg/h;
(5) after regulating the first control valve 2 and the 4th control valve 17, the nitrogen of-145 DEG C reduces to-190 DEG C through the second decompressor 13 temperature, pressure reduces to 0.13MPa, enter in the second heat exchanger 14, with the BOG heat exchange coming from LNG storage tank 16, be back in LNG storage tank 16 through pump 15 after making it be liquefied as LNG, nitrogen is then warming up to-155 DEG C, return in First Heat Exchanger 12, by cold supply 22 DEG C, 0.8MPa, 730kg/h(584Nm from the second control valve 6
3/ h) nitrogen, this strand of nitrogen temperature is made to reduce to-145 DEG C, own temperature gos up to return in nitrogen storage tank 1 after 18 DEG C, after the first compressor 4 and the first water cooling heat exchanger 5, temperature becomes 22 DEG C again,-145 DEG C are reduced to through First Heat Exchanger 12 temperature, enter the second decompressor 13 and expand cooling for-190 DEG C, cold is passed to the BOG coming from LNG storage tank 16 in the second heat exchanger 14 and make its recovery of liquefying, circulate according to this and continuously reclaim BOG.
Above parameter is the value of ideal or optimum state, and because of affected by environment during practical operation, those skilled in the art can do corresponding adjustment, to reach the object reclaiming BOG.
Claims (5)
1. reclaim a technique of BOG, it is characterized in that coming from the nitrogen compression of nitrogen storage tank, obtain high pressure nitrogen, high pressure nitrogen enters BOG reclaiming system; In BOG reclaiming system, high pressure nitrogen, through water-cooled heat exchange, obtains cryogenic high pressure nitrogen; Cryogenic high pressure nitrogen reflation is to atmospheric pressure state, temperature reduces further, the cold supply of being contained by this part nitrogen comes from the BOG of LNG storage tank, BOG is liquefied, nitrogen is back to nitrogen storage tank after temperature recovery in BOG reclaiming system, and the nitrogen being back to nitrogen storage tank circulates aforesaid manufacturing process again; The technique of described recovery BOG, is characterized in that comprising the following steps:
(1) first control valve (2), the 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, the nitrogen of 15 ~ 25 DEG C are exported by nitrogen storage tank (1), enter the first compressor (4), be compressed to 0.3 ~ 0.8MPa, temperature becomes 120 ~ 290 DEG C, then the first water cooling heat exchanger (5) is entered, with 10 ~ 15 DEG C, the water heat exchange of 0.1 ~ 0.2MPa, nitrogen temperature reduces to 20 ~ 30 DEG C;
The nitrogen of (2) 20 ~ 30 DEG C is divided into two strands, and one flows through the second control valve (6), and one flows through the 3rd control valve (7); The nitrogen wherein flowing through the 3rd control valve (7) is introduced into the second compression (8) increasing temperature and pressure, then the second water cooling heat exchanger (9) cooling is entered, expand through the first decompressor (10) again, temperature reduces to-120 ~-130 DEG C, pressure reduces to 0.1 ~ 0.2MPa, flow to the cold logistics import of First Heat Exchanger (12);
(3) the hot stream outlet of 20 ~ 30 DEG C of nitrogen from First Heat Exchanger (12) after First Heat Exchanger (12) heat exchange cooling flowing through the second control valve (6) flows out, expand through the second decompressor (13) again and lower the temperature, pressure reduces to 0.1 ~ 0.2MPa, the cold logistics import of First Heat Exchanger (12) is flow to through the 5th control valve (19), one is combined into the first decompressor (10) nitrogen out, enter First Heat Exchanger (12) heat exchange, temperature is increased to 15 ~ 25 DEG C and returns nitrogen storage tank (1);
(4) when the nitrogen of 20 ~ 30 DEG C from the second control valve (6) is after First Heat Exchanger (12) heat exchange cooling, when temperature remains on-140 ~-150 DEG C, 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 the first control valve (2), the nitrogen flow controlling to flow out nitrogen storage tank 1 is identical with the nitrogen flow flowing through the second control valve (6) in step (2);
(5) nitrogen of described-140 ~-150 DEG C expands cooling for-180 ~-195 DEG C through the second decompressor (13), cold is passed to the BOG coming from LNG storage tank (16) in the second heat exchanger (14) and make its recovery of liquefying, nitrogen temperature gos up to-150 ~-170 DEG C, be back to the cold logistics import of First Heat Exchanger (12), in First Heat Exchanger (12), the nitrogen from the second control valve (6) is cooled to-140 ~-150 DEG C, own temperature is increased to 15 ~ 25 DEG C and returns nitrogen storage tank (1), after the first compressor (4) and the first water cooling heat exchanger (5), temperature reduces to 20 ~ 30 DEG C again,-140 ~-150 DEG C are reduced to through First Heat Exchanger (12) temperature, enter the second decompressor (13) and expand cooling for-180 ~-195 DEG C, cold is passed to the BOG coming from LNG storage tank (16) in the second heat exchanger (14) and make its recovery of liquefying, circulate according to this and continuously reclaim BOG.
2. a kind of technique reclaiming BOG according to claim 1, it is characterized in that for described first compressor (4) and the running of the second decompressor (13) connecting shaft, second compressor (8) and the running of the first decompressor (10) connecting shaft, expansion work directly supplies compressor, compressor connects power supply simultaneously, is supplemented the electric power of needs by externally fed.
3. realize the device of the technique reclaiming BOG described in claim 1 or 2, 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-class gauge (3), second gauge (11), 3rd flowmeter (18), first control valve (2), second control valve (6), 3rd control valve (7), 4th control valve (17), 5th control valve (19), 6th control valve (20), described nitrogen storage tank (1) is connected by the first control valve (2) and first-class gauge (3) with the first compressor (4), the outlet of the first compressor (4) is connected with the hot logistics import of the first water cooling heat exchanger (5), the hot stream outlet bifurcation of the first water cooling heat exchanger (5), one is connected with the import of the second compressor (8) by the 3rd control valve (7), and another is connected with the hot logistics import of second gauge (11) first water cooling heat exchanger (5) by the second control valve (6), the outlet of the second compressor (8) is connected with the hot logistics import of the second water cooling heat exchanger (9), the outlet of hot logistics is connected with the import of the first decompressor (10), the outlet of the first decompressor (10) is connected with the cold logistics import of First Heat Exchanger (12), First Heat Exchanger (12) cold stream outlet is connected with the import of nitrogen storage tank (1), the outlet of hot logistics is connected with the import of the second decompressor (13), the outlet of the second decompressor (13) separates two, one is connected with the cold logistics import of First Heat Exchanger (12) by the 5th control valve (19), another is connected by the 6th control valve (20) with the cold logistics import of the second heat exchanger (14), the cold stream outlet of the 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 the second heat exchanger (14) with the 3rd flowmeter (18) by the 4th control valve (17), hot stream outlet is then connected with the import of pump (15), the outlet of pump (15) is connected with the import of LNG storage tank (16).
4. device according to claim 3, is characterized in that, the cold logistics import of described First Heat Exchanger (12) is connected by hot insulated line with the outlet of the first decompressor (10); Hot stream outlet is connected by hot insulated line with the import of the second decompressor (13); The outlet of the second decompressor (13) is connected by hot insulated line with the cold logistics import of the second heat exchanger (14); The outlet of LNG storage tank (16) is connected by hot insulated line with the hot logistics import of the second heat exchanger (14); The hot stream outlet of the second heat exchanger (14) is all 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).
5. device according to claim 3, 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 |
| CN104482395B (en) * | 2014-11-05 | 2016-05-18 | 中海福建天然气有限责任公司 | A kind of method of BOG while utilizing LNG cold energy to reclaim tank car entrucking |
| CN104482396B (en) * | 2014-11-11 | 2017-02-01 | 南京工业大学 | BOG recovery system with cold storage function |
| 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 |
| CN106051459B (en) * | 2016-07-14 | 2018-08-21 | 青岛华控能源科技有限公司 | Tire nitrogen vulcanizes two-step supercharging and recycles energy conserving system |
| 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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