CN204757540U - BOG purifies liquefaction recovery unit - Google Patents
BOG purifies liquefaction recovery unit Download PDFInfo
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- CN204757540U CN204757540U CN201520490973.8U CN201520490973U CN204757540U CN 204757540 U CN204757540 U CN 204757540U CN 201520490973 U CN201520490973 U CN 201520490973U CN 204757540 U CN204757540 U CN 204757540U
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of 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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead gas
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/90—Boil-off gas from storage
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- F25J2270/18—External refrigeration with incorporated cascade loop
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/66—Closed external refrigeration cycle with multi component refrigerant [MCR], e.g. mixture of hydrocarbons
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/34—Details about subcooling of liquids
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/40—Vertical layout or arrangement of cold equipments within in the cold box, e.g. columns, condensers, heat exchangers etc.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Filling Or Discharging Of Gas Storage Vessels (AREA)
Abstract
BOG purifies liquefaction recovery unit is including cooling cycle system and BOG clean system, cooling cycle system includes the cold box, has cooling runner and cold source recovery runner in the cold box, and the cooling runner divide into precooling section, cryrogenic section, first subcooling section and second subcooling section, BOG clean system includes scrubbing tower, first flash tank, second flash tank, first choke valve, second choke valve and low temperature backwash pump. The utility model discloses when making liquefied natural gas with BOG liquefaction, high -load nitrogen gas in can desorption BOG and the micro - hydrogen that wherein probably exists. Because the high integrated nature of this equipment can effectively reduce cold the damage, improve BOG's liquefaction efficiency simultaneously. And the utilization of energy is taken all factors into consideration to this device, can effectively reduce the energy consumption.
Description
Technical field
The utility model relates to liquefied natural gas field, relates in particular to a kind of BOG and purifies recovery device of liquefied.
Background technology
BOG (BoilOffGas) refers to the part boil-off gas that liquefied natural gas volatilizees due to heat absorption, and the BOG of liquefied natural gas mainly results from four aspects: one, the daily evaporation of low-temperature storage tank of liquefied natural gas; Two, the entrucking operation of liquefied natural gas (LNG) plant loading station; The recovery of BOG in car when three, LNG tank car starts entrucking; Four, the charge and discharge operations of coastal, riverine liquefied natural gas receiving station.The content of the methane in BOG is about 80%-90%, and nitrogen content is about 10%-15%, also may have micro-propane and ethane etc.
Liquefied natural gas (Liquefiednaturalgas is abbreviated as LNG) is natural gas via pressure regulation metering, the liquid that becomes after purification and liquefaction unit operation.Liquefied natural gas storage condition normally at ambient pressure about-161 DEG C, compared with compressed natural gas, liquefied natural gas is convenient to store, transport and use, and security improves greatly, the terminal sale of LNG is also not limited to Vehicle Fueling Station, can sell to the users such as industry and commerce.
Although there is nitrogen in BOG, still containing a large amount of methane, BOG normally burns or emptying as fuel gas in the processing mode of liquefied natural gas (LNG) plant, and the part BOG for emptying is actually the serious wasting of resources.Therefore design a kind of purify and the device of the recovery BOG that liquefies will avoid the wasting of resources, and be conducive to the utilization of resource.
Utility model content
Technical problem to be solved in the utility model is to provide a kind of BOG and purifies recovery device of liquefied, and this device effectively can remove the assorted gas in BOG, and BOG can be made liquefied natural gas recovery.
In order to solve the problems of the technologies described above, the utility model adopts following technical scheme: BOG purifies recovery device of liquefied, comprises cooling cycle system and BOG cleaning system;
Described cooling cycle system comprises ice chest, and have coolant flow channel and low-temperature receiver recovery runner in ice chest, coolant flow channel is divided into precooling zone, cryogenic, the first super cooled sect and the second super cooled sect;
Described BOG cleaning system comprises scrubbing tower, the first flash tank, the second flash tank, first throttle valve, second throttle and low temperature reflux pump, unstripped gas enters from one end of precooling zone, the other end of precooling zone is connected with one end of cryogenic, the other end of cryogenic is connected with the bottom feed mouth of scrubbing tower through first throttle valve, the bottom discharge mouth of scrubbing tower is connected with one end of the first super cooled sect, the other end of the first super cooled sect is connected through the charging aperture of second throttle with the first flash tank, the top discharge mouth of scrubbing tower is connected with one end of the second super cooled sect, the other end of the second super cooled sect is connected with the charging aperture of the second flash tank, one end that top discharge mouth and the low-temperature receiver of the second flash tank reclaim runner is connected, the bottom discharge mouth of the second flash tank is connected with its top feed mouth of scrubbing tower through low temperature reflux pump.
Further, described cooling cycle system also comprises cryogen suction tank, compressor, cryogen cooler, first cryogen divides flow container, gas phase cryogen choke valve, liquid phase cryogen choke valve, and the first refrigerant flow conduit be located in ice chest, second refrigerant flow conduit, 3rd refrigerant flow conduit and the second cryogen divide flow container, first cryogen divides the liquid outlet of flow container to be connected with one end of the 3rd refrigerant flow conduit, the other end of the 3rd refrigerant flow conduit is connected with the middle part of the first refrigerant flow conduit through liquid phase cryogen choke valve, first cryogen divides the gas outlet of flow container to be connected with one end of the second refrigerant flow conduit, the other end of the second refrigerant flow conduit divides the import of flow container to be connected through gas phase cryogen choke valve and the second cryogen, second cryogen divides the gas outlet of flow container and liquid outlet to be all connected with one end of the first refrigerant flow conduit, the other end of the first refrigerant flow conduit is successively through cryogen suction tank, compressor divides the import of flow container to be connected with cryogen cooler and the first cryogen.
Further, described precooling zone, cryogenic, the first super cooled sect are identical with the circulating direction of the second super cooled sect, and the circulating direction that low-temperature receiver reclaims runner is contrary with the circulating direction of precooling zone.
Further, scrubbing tower and the second flash tank are connected to become a whole, and what scrubbing tower was connected with the second flash tank is monolithically integrated in cold box interior.
The beneficial effects of the utility model are: the utility model by BOG liquefaction make liquefied natural gas while, the trace hydrogen that can remove the high-load nitrogen in BOG and wherein may exist.Simultaneously due to the high integration of this equipment, cold damage can be effectively reduced, improve the liquefaction efficiency of BOG.And this device considers Energy harvesting, energy consumption can be effectively reduced.
Accompanying drawing explanation
Fig. 1 is the structural representation of the utility model one embodiment.
Being labeled as of each parts in accompanying drawing: 1 cryogen suction tank, 2 compressors, 3 cryogen coolers, 4 first cryogens divide flow container, 5 first flash tanks, 6 second flash tanks, 7 low temperature reflux pumps, 8 scrubbing towers, 9 second cryogens divide flow container, 10 ice chests, c1 precooling zone, c2 cryogenic, c3 first super cooled sect, c4 second super cooled sect, c5 low-temperature receiver reclaims runner, L1 first refrigerant flow conduit, L2 second refrigerant flow conduit, L3 the 3rd refrigerant flow conduit, v1 first throttle valve, v2 second throttle, v3 gas phase cryogen choke valve, v4 liquid phase cryogen choke valve.
Detailed description of the invention
Below in conjunction with accompanying drawing, the utility model is further described:
See Fig. 1.
The BOG of the utility model one embodiment purifies recovery device of liquefied, comprises cooling cycle system and BOG cleaning system;
Described cooling cycle system comprises ice chest 10, and have coolant flow channel and low-temperature receiver recovery runner c5 in ice chest 10, coolant flow channel is divided into precooling zone c1, cryogenic c2, the first super cooled sect c3 and the second super cooled sect c4;
Described BOG cleaning system comprises scrubbing tower 8, first flash tank 5, second flash tank 6, first throttle valve v1, second throttle v2 and low temperature reflux pump 7, unstripped gas enters from one end of precooling zone c1, the other end of precooling zone c1 is connected with one end of cryogenic c2, the other end of cryogenic c2 is connected with the bottom feed mouth of scrubbing tower 8 through first throttle valve v1, the bottom discharge mouth of scrubbing tower 8 is connected with one end of the first super cooled sect c3, the other end of the first super cooled sect c3 is connected with the charging aperture of the first flash tank 5 through second throttle v2, the top discharge mouth of scrubbing tower 8 is connected with one end of the second super cooled sect c4, the other end of the second super cooled sect c4 is connected with the charging aperture of the second flash tank 6, one end that top discharge mouth and the low-temperature receiver of the second flash tank 6 reclaim runner c5 is connected, the bottom discharge mouth of the second flash tank 6 is connected with its top feed mouth of scrubbing tower 8 through low temperature reflux pump 7.
Described cooling cycle system also comprises cryogen suction tank 1, compressor 2, cryogen cooler 3, first cryogen divides flow container 4, gas phase cryogen choke valve v3, liquid phase cryogen choke valve v4, and the first refrigerant flow conduit L1 be located in ice chest 10, second refrigerant flow conduit L2, 3rd refrigerant flow conduit L3 and the second cryogen divide flow container 9, first cryogen divides the liquid outlet of flow container 4 to be connected with one end of the 3rd refrigerant flow conduit L3, the other end of the 3rd refrigerant flow conduit L3 is connected with the middle part of the first refrigerant flow conduit L1 through liquid phase cryogen choke valve v4, first cryogen divides the gas outlet of flow container 4 to be connected with one end of the second refrigerant flow conduit L2, the other end of the second refrigerant flow conduit L2 divides the import of flow container 9 to be connected through gas phase cryogen choke valve v3 with the second cryogen, second cryogen divides the gas outlet of flow container 9 and liquid outlet to be all connected with one end of the first refrigerant flow conduit L1, the other end of the first refrigerant flow conduit L1 is successively through cryogen suction tank 1, compressor 2 divides the import of flow container 4 to be connected with cryogen cooler 3 and the first cryogen.
Described precooling zone c1, cryogenic c2, the first super cooled sect c3 are identical with the circulating direction of the second super cooled sect c4, and the circulating direction that low-temperature receiver reclaims runner c5 is contrary with the circulating direction of precooling zone c1.Adopt above structure, low-temperature receiver organic efficiency can be improved.In the present embodiment, first refrigerant flow conduit L1, second refrigerant flow conduit L2, 3rd refrigerant flow conduit L3, precooling zone c1, cryogenic c2, first super cooled sect c3, second super cooled sect c4 and low-temperature receiver reclaim runner c5 and line up 5 rows by same direction in ice chests 10, wherein, from left to right, first refrigerant flow conduit L1 is at first row, second refrigerant flow conduit L2 is at second row, low-temperature receiver reclaims runner c5 the 3rd row, 3rd refrigerant flow conduit L3 is at the first half of the 4th row, first super cooled sect c3 is in the Lower Half of the 4th row, 5th row is precooling zone c1 under upper, cryogenic c2 and the second super cooled sect c4.
Scrubbing tower 8 and the second flash tank 6 are connected to become a whole, and what scrubbing tower 8 was connected with the second flash tank 6 is monolithically integrated in ice chest 10 inside.Adopt above structure, integration of the present utility model can be improved further.
The course of work of the BOG purification recovery device of liquefied of the utility model one embodiment is:
By the first supercharging of BOG unstripped gas of reclaiming, after cooling, send into precooling zone c1, the operating pressure of precooling zone c1 is at more than 3.5MPag, cryogenic c2 is entered after BOG is cooled to (-40)-(-50) DEG C in precooling zone, more than operating pressure 3.5MPag, BOG is reduced to (-80)-(-100) DEG C in cryogenic c2, then BOG discharges and bottom feed mouth from scrubbing tower 8 after first throttle valve v1 is decompressed to 0.5-1.5MPag enters in cryogenic c2, wash from bottom to top, the operating pressure of scrubbing tower 8 is 0.5-1.5MPag, temperature (-110)-(-130) DEG C, BOG after washing discharges from the bottom discharge mouth of scrubbing tower 8 and introduces the first super cooled sect c3, the operating pressure of the first super cooled sect c3 is 0.5-1.5MPag, discharge after BOG is cooled to (-150)-(-165) DEG C in the first super cooled sect c3 and enter in the first flash tank 5 through second throttle v2, the operating pressure of the first flash tank 5 is 0-1MPag, after flash distillation, the liquid product that the bottom of the first flash tank 5 is flowed out is target liquefied natural gas product, can enter in LNG storage tank and store, the gas-phase product flashed off on a small quantity is discharged from the top of the first flash tank 5, and the product that the top discharge mouth of scrubbing tower 8 is discharged enters the second super cooled sect c4, operating pressure 0.5-the 1.5MPag of the second super cooled sect c4, discharge be cooled to (-150)-(-165) DEG C in the second super cooled sect c4 after and introduce the second flash tank 6, after flash distillation, the liquid product of the bottom outflow of the second flash tank 6 is delivered to its top feed mouth of scrubbing tower 8 through low temperature reflux pump 7, wash from top to bottom, the gas-phase product of the second flash tank 6 enters low-temperature receiver and reclaims runner c5 and reclaim the discharge of runner c5 adverse current from low-temperature receiver, as low-temperature receiver recovery section cold, and the gas-phase product of discharging can be used as fuel gas and uses.
The low-temperature receiver of ice chest 10 is provided by cooling cycle system, during use, cold-producing medium divides in flow container 4 at the first cryogen and carries out gas-liquid separation, the liquid phase refrigerant of gained enters from one end of the 3rd refrigerant flow conduit L3, discharge from the other end of rear 3rd refrigerant flow conduit L3 after heat exchange, then enter from the middle part of the first refrigerant flow conduit L1 after liquid phase cryogen choke valve v4 reduces pressure, and the first cryogen divides the vapor phase refrigerant of flow container 4 gained to enter from one end of the second refrigerant flow conduit L2, discharge from the other end of the second refrigerant flow conduit L2 after heat exchange, then after gas phase cryogen choke valve v3 reduces pressure, enter the second cryogen to divide in flow container 9 and carry out gas-liquid separation, the gas phase of gained and liquid phase refrigerant enter from one end of the first refrigerant flow conduit L1 respectively, escape and enter in cryogen suction tank 1 from the other end of the first refrigerant flow conduit L1 after above-mentioned gas phase and liquid phase refrigerant carry out heat exchange in the first refrigerant flow conduit L1, compress finally by compressor 2, cryogen cooler 3 comes back to the first cryogen after cooling and divides in flow container 4, by the compression of cold-producing medium iterative cycles, cooling, throttling expansion realizes the cooling to ice chest.
After BOG first throttle valve v1 is decompressed to 0.5-1.5MPag, temperature reaches (-110-(-130) DEG C, wash in scrubbing tower 8 at this temperature, and methane is in a liquid state at this temperature and pressure, hydrogen, nitrogen are gaseous state, so liquid methane can be washed out from wash tower bottoms by energy exchange in scrubbing tower 8, nitrogen, hydrogen then become gaseous state to go out tower from scrubbing tower top, thus reach the object of trace hydrogen being separated high-load nitrogen in BOG and may existing.
In the first super cooled sect c3, the pressure of liquefied natural gas product is out about 1MPag, because LNG stores under atmospheric pressure state, so need to utilize second throttle v2 to carry out decompression operation before entering the first flash tank 5, if the pressure of liquefied natural gas product maintains more than 80Kpg after decompression, then do not have BOG to produce, if the pressure of liquefied natural gas product maintains below 60Kpg after decompression, then may have a small amount of BOG in decompression process to produce, the object arranging the first flash tank 5 is exactly that the liquefied natural gas that may exist after the decompression operation of second throttle v2 is carried out gas-liquid separation, obtain the liquefied natural gas product of pure liquid phase.
Be to be understood that example as herein described and embodiment only in order to illustrate; those skilled in the art can make various amendment or change according to it; when not departing from the utility model Spirit Essence, all belong to protection domain of the present utility model, as scrubbing tower can substitute with washing tank.
Claims (4)
1.BOG purifies recovery device of liquefied, it is characterized in that: comprise cooling cycle system and BOG cleaning system;
Described cooling cycle system comprises ice chest (10), have coolant flow channel and low-temperature receiver recovery runner (c5) in ice chest (10), coolant flow channel is divided into precooling zone (c1), cryogenic (c2), the first super cooled sect (c3) and the second super cooled sect (c4);
Described BOG cleaning system comprises scrubbing tower (8), the first flash tank (5), the second flash tank (6), first throttle valve (v1), second throttle (v2) and low temperature reflux pump (7), unstripped gas enters from the one end of precooling zone (c1), the other end of precooling zone (c1) is connected with one end of cryogenic (c2), the other end of cryogenic (c2) is connected through the bottom feed mouth of first throttle valve (v1) with scrubbing tower (8), the bottom discharge mouth of scrubbing tower (8) is connected with one end of the first super cooled sect (c3), the other end of the first super cooled sect (c3) is connected through the charging aperture of second throttle (v2) with the first flash tank (5), the top discharge mouth of scrubbing tower (8) is connected with one end of the second super cooled sect (c4), the other end of the second super cooled sect (c4) is connected with the charging aperture of the second flash tank (6), one end that top discharge mouth and the low-temperature receiver of the second flash tank (6) reclaim runner (c5) is connected, the bottom discharge mouth of the second flash tank (6) is connected through its top feed mouth of low temperature reflux pump (7) with scrubbing tower (8).
2. BOG as claimed in claim 1 purifies recovery device of liquefied, it is characterized in that: described cooling cycle system also comprises cryogen suction tank (1), compressor (2), cryogen cooler (3), first cryogen divides flow container (4), gas phase cryogen choke valve (v3), liquid phase cryogen choke valve (v4), and the first refrigerant flow conduit (L1) be located in ice chest (10), second refrigerant flow conduit (L2), 3rd refrigerant flow conduit (L3) and the second cryogen divide flow container (9), first cryogen divides the liquid outlet of flow container (4) to be connected with one end of the 3rd refrigerant flow conduit (L3), the other end of the 3rd refrigerant flow conduit (L3) is connected through the middle part of liquid phase cryogen choke valve (v4) with the first refrigerant flow conduit (L1), first cryogen divides the gas outlet of flow container (4) to be connected with one end of the second refrigerant flow conduit (L2), the other end of the second refrigerant flow conduit (L2) divides the import of flow container (9) to be connected through gas phase cryogen choke valve (v3) and the second cryogen, second cryogen divides the gas outlet of flow container (9) and liquid outlet to be all connected with one end of the first refrigerant flow conduit (L1), the other end of the first refrigerant flow conduit (L1) is successively through cryogen suction tank (1), compressor (2) and cryogen cooler (3) and the first cryogen divide the import of flow container (4) to be connected.
3. BOG as claimed in claim 1 or 2 purifies recovery device of liquefied, it is characterized in that: described precooling zone (c1), cryogenic (c2), the first super cooled sect (c3) are identical with the circulating direction of the second super cooled sect (c4), the circulating direction that low-temperature receiver reclaims runner (c5) is contrary with the circulating direction of precooling zone (c1).
4. BOG as claimed in claim 1 or 2 purifies recovery device of liquefied, it is characterized in that: scrubbing tower (8) and the second flash tank (6) are connected to become a whole, what scrubbing tower (8) was connected with the second flash tank (6) is monolithically integrated in ice chest (10) inside.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520490973.8U CN204757540U (en) | 2015-07-07 | 2015-07-07 | BOG purifies liquefaction recovery unit |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201520490973.8U CN204757540U (en) | 2015-07-07 | 2015-07-07 | BOG purifies liquefaction recovery unit |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CN204757540U true CN204757540U (en) | 2015-11-11 |
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| CN201520490973.8U Expired - Fee Related CN204757540U (en) | 2015-07-07 | 2015-07-07 | BOG purifies liquefaction recovery unit |
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Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107548446A (en) * | 2015-05-04 | 2018-01-05 | 通用电气石油和天然气公司 | Prepare the hydrocarbon stream for storage |
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107548446A (en) * | 2015-05-04 | 2018-01-05 | 通用电气石油和天然气公司 | Prepare the hydrocarbon stream for storage |
| US10928128B2 (en) | 2015-05-04 | 2021-02-23 | GE Oil & Gas, Inc. | Preparing hydrocarbon streams for storage |
| US11988445B2 (en) | 2015-05-04 | 2024-05-21 | GE Oil & Gas, Inc. | Preparing hydrocarbon streams for storage |
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