CN2766203Y - Air separator for recovering cold energy of liquefied natural gas - Google Patents
Air separator for recovering cold energy of liquefied natural gas Download PDFInfo
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- CN2766203Y CN2766203Y CNU2005202003068U CN200520200306U CN2766203Y CN 2766203 Y CN2766203 Y CN 2766203Y CN U2005202003068 U CNU2005202003068 U CN U2005202003068U CN 200520200306 U CN200520200306 U CN 200520200306U CN 2766203 Y CN2766203 Y CN 2766203Y
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- heat exchanger
- air
- nitrogen
- natural gas
- liquefied natural
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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
- F25J3/04—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 for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
- F25J3/0426—The cryogenic component does not participate in the fractionation
- F25J3/04266—The cryogenic component does not participate in the fractionation and being liquefied 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
- 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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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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
- F25J3/04—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 for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams 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
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- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04157—Afterstage cooling and so-called "pre-cooling" of the feed air upstream the air purification unit and main heat exchange line
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
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- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
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- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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- 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
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- F25J3/04—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 for air
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- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen
- F25J3/04357—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams of nitrogen and comprising a gas work expansion 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
- 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
- F25J3/04—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 for air
- F25J3/04406—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 for air using a dual pressure main column system
- F25J3/04412—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 for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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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
- F25J3/04—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 for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
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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
- F25J3/04—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 for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
- F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
- F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
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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
- F25J3/04—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 for air
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
- F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
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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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
- F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
- F25J2205/70—Heating the adsorption vessel
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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
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- F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
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- Engineering & Computer Science (AREA)
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- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The utility model relates to an air separator for recovering cold energy of liquefied natural gas, which comprises a nitrogen gas refrigerating circulation device using liquefied natural gas cold energy for pre-cooling, an air liquefying separation device, an air cooler and an air liquefier which are used for connecting the nitrogen gas refrigerating circulation device with the air liquefying separation device, a group of needed valves and connecting pipelines which are used for starting and normal running. The air separator also adopts a low temperature air compressor, a low temperature nitrogen gas supercharger, a supercharging expander, a throttling valve and an air precooler which uses the waste cold of pure nitrogen and waste nitrogen for cooling feedstock air, etc. The utility model can be used for recovering the cold energy of liquefied natural gas effectively to reduce operating cost and environment pollution, and can greatly reduce electricity and water consumption in the process of producing liquefied products.
Description
Technical field
The utility model relates to a kind of air-separating plant that reclaims cold energy of liquefied natural gas.
Technical background
Liquefied natural gas (LNG) is a kind of high-grade energy, has characteristics such as calorific value height, cleaning, Air are little, and contains a large amount of high-grade low temperature colds (temperature of LNG is generally at 150 ℃～160 ℃ behind the high-pressure pump of LNG station).Normally absorb this partly cold during liquefied natural gas vaporization with seawater, again seawater is discharged in the sea and goes, a large amount of colds have so not only been wasted, and cause local marine site low temperature to pollute, so how to reclaim and rationally utilize this considerable cold just to become that people extremely are concerned about when using liquefied natural gas (LNG) and the problem of exploration for it.
Air-separating plant is to be raw material with the air, makes it to separate according to the different boiling of gases such as oxygen, nitrogen, argon gas, thereby produces the equipment of gases such as gaseous state or liquid oxygen, nitrogen, argon gas.They are widely used in fields such as metallurgy, petrochemical industry, machinery, chemical fertilizer, glass, military project, food, medical treatment.But common air-separating plant energy consumption is big, and during especially for production liquid gas, energy consumption will increase exponentially.Along with the sustainable development of national economy, the maximization and the air separation liquid form product demand of air-separating plant increased sharply.Be tending towards short today day by day at the energy, the contradiction of a large amount of energy consumptions will be more outstanding.How reducing it and consume, is the problem that people extremely are concerned about and explore for it equally.
Summary of the invention
The purpose of this utility model is to provide a kind of air-separating plant that reclaims cold energy of liquefied natural gas and be used to produce liquid gases such as liquid oxygen, liquid nitrogen, liquid argon, this device not only can effectively reclaim the cold energy of liquefied natural gas, reduce operating cost and environmental pollution, and when producing liquid form product, can reduce power consumption and water consumption significantly.
The air-separating plant that is used to reclaim cold energy of liquefied natural gas of the present utility model, comprise with cold energy of liquefied natural gas do precooling nitrogen refrigerating circulatory device, air liquefaction separation, be used to connect nitrogen refrigerating circulatory device and air liquefaction separation aerial cooler 9 and air liquefier 10, be used to start and normally move required one group of valve and connecting line, it is characterized in that:
1.1 press circulating nitrogen gas heat exchanger channels S12 → S13 and raw air heat exchanger channels S14 → S15 in being provided with in the described aerial cooler 9, hydraulic fluid nitrogen heat exchanger channels S16 → S17 and raw air heat exchanger channels S18 → S19 in being provided with in the described air liquefier 10;
1.2 described nitrogen refrigerating circulatory device comprises liquefied natural gas basin 1, liquefied natural gas booster pump 2, the circularly-supercharged machine 3 of low temperature nitrogen, expansion-supercharger 4, liquefied natural gas heat exchanger 5, cryogenic heat exchanger 6, supercharging-decompressor 7, choke valve J1, gas-liquid separator 8 and connecting line thereof;
1.2.1 be provided with liquefied natural gas heat exchanger channels S1 → S2, cycle of higher pressure nitrogen heat exchanger channels S3 → S4 and middle pressure circulating nitrogen gas heat exchanger channels S5 → S6 in the described liquefied natural gas heat exchanger 5;
1.2.2 be provided with cycle of higher pressure nitrogen heat exchanger channels S4 → S7 and middle pressure circulating nitrogen gas heat exchanger channels S8 → S9 in the described cryogenic heat exchanger 6;
1.3 described air liquefaction separation comprises air cleaner 11, air compressor 12, air precooler 13, molecular sieve purifier 14, Cryogenic air compressor 15, main heat exchanger 16, goes up tower 17, condenser/evaporator 18, following tower 19, subcooler 20, crude argon column 21-1, crude argon column 21-2, circulation liquid argon pump 22, pure argon column 23, liquid oxygen storage tank 24, liquid nitrogen storage 25, liquid argon storage tank 26;
1.3.1 purity nitrogen passage S25 → S26 that described air precooler 13 is provided with the enterprising raw air passage S21 → S22 that goes out down, the dirty nitrogen passage S23 → S24 that goes out on advancing down, goes out on advancing down;
1.3.2 be provided with in the described main heat exchanger 16 the enterprising raw air heat exchanger channels S18 → S29 that goes out down, the dirty nitrogen passage S30 → S23 that goes out on advancing down, the purity nitrogen passage S31 → S25 that goes out on advancing down and in press channel of nitrogen S32 → S17;
1.4 the order of connection of described nitrogen refrigerating circulatory device is: begin from middle pressure nitrogen inlet S11, meet the middle pressure circulating nitrogen gas heat exchanger channels S5 → S6 in the liquefied natural gas heat exchanger 5, connect the circularly-supercharged machine 3 of low temperature nitrogen, connect expansion-supercharger 4, meet the cycle of higher pressure nitrogen heat exchanger channels S3 → S4 of liquefied natural gas heat exchanger 5, after interface S4, be divided into two-way; One the tunnel connects supercharging-decompressor 7, and another road meets the cycle of higher pressure nitrogen heat exchanger channels S4 → S7 in the cryogenic heat exchanger 6, after choke valve J1 and the first via are intersected in S10, is connected to gas-liquid separator 8 again; The top exit S12 of described gas-liquid separator meets the middle pressure circulating nitrogen gas heat exchanger channels S8 → S9 in the cryogenic heat exchanger 6, is intersected in nitrogen inlet S11 after meeting the middle pressure circulating nitrogen gas heat exchanger channels S12 → S13 in the aerial cooler 9 again; The outlet at bottom S20 of described gas-liquid separator divides two-way to go out, and one the tunnel is connected to the following tower S28 of air separation unit, the middle hydraulic fluid nitrogen heat exchanger channels S16 → S17 of another road in breather valve T3 is connected to air liquefier 10 through breather valve T2; After described natural gas basin 1 connects liquefied natural gas booster pump 2, meet the liquefied natural gas heat exchanger channels S1 → S2 in the liquefied natural gas heat exchanger 5.
1.5 the order of connection of described air-separating plant is: n1 begins from air intlet, connect air cleaner 11, connect air compressor 12, meet the enterprising raw air passage S21 → S22 that goes out down in the air precooler 13, connect molecular sieve purifier 14, again behind the raw air heat exchanger channels S14 → S15 in aerial cooler 9, connect Cryogenic air compressor 15 backs and divide two-way, one the tunnel meets the raw air heat exchanger channels S18 → S19 in the air liquefier 10, connect down tower 19 again, another road meets the enterprising raw air heat exchanger channels S18 → S29 that goes out down in the main heat exchanger 16, is connected to down tower S29 again; Through reconnecting tower 17, crude argon column 21-1 behind the tower 19 down, crude argon column 21-2, pure argon column 23 are connected with circulation liquid argon pump 22 between described crude argon column 21-1 and the crude argon column 21-2, connect liquid oxygen storage tank 24, liquid nitrogen storage 25, liquid argon storage tank 26 at last.
On the basis of above-mentioned technology, the utility model can also omit aerial cooler 9 and Cryogenic air compressor 15, and node S6 and S9 are merged into node S6; Node S14 and S18 are merged into node S14.
Advantage of the present utility model is: the one, to compare with the air separation unit of traditional production liquid form product, and the utility model can economize on electricity about 60%, and water saving is more than 90%; If adopt second kind technical scheme, can economize on electricity more than 50%, water saving is more than 70%; The 2nd, can save the seawater of the liquefied natural gas that is used in a large number to vaporize and reduce low temperature seawater and inject in the sea that the low temperature in caused local marine site pollutes; The 3rd, owing to taked the multiple LNG of preventing to invade the empty measure that divides distillation system, the safe and reliable operation of air separation unit can well be guaranteed; The 4th, compact conformation, cost is low.
Description of drawings
Fig. 1 is the schematic flow sheet of the utility model embodiment one.
Fig. 2 is the schematic flow sheet of the utility model embodiment two.
The specific embodiment
Embodiment one:
The utility model comprise with cold energy of liquefied natural gas do precooling nitrogen refrigerating circulatory device, air liquefaction separation, be used to connect nitrogen refrigerating circulatory device and air liquefaction separation aerial cooler 9 and air liquefier 10, be used to start and normally move required one group of valve and connecting line, it is characterized in that:
1.1 press circulating nitrogen gas heat exchanger channels S12 → S13 and raw air heat exchanger channels S14 → S15 in being provided with in the described aerial cooler 9, hydraulic fluid nitrogen heat exchanger channels S16 → S17 and raw air heat exchanger channels S18 → S19 in being provided with in the described air liquefier 10;
1.2 described nitrogen refrigerating circulatory device comprises liquefied natural gas basin 1, liquefied natural gas booster pump 2, the circularly-supercharged machine 3 of low temperature nitrogen, expansion-supercharger 4, liquefied natural gas heat exchanger 5, cryogenic heat exchanger 6, supercharging-decompressor 7, choke valve J1, gas-liquid separator 8 and connecting line thereof;
1.2.1 be provided with liquefied natural gas heat exchanger channels S1 → S2, cycle of higher pressure nitrogen heat exchanger channels S3 → S4 and middle pressure circulating nitrogen gas heat exchanger channels S5 → S6 in the described liquefied natural gas heat exchanger 5;
1.2.2 be provided with cycle of higher pressure nitrogen heat exchanger channels S4 → S7 and middle pressure circulating nitrogen gas heat exchanger channels S8 → S9 in the described cryogenic heat exchanger 6;
1.3 described air liquefaction separation comprises air cleaner 11, air compressor 12, air precooler 13, molecular sieve purifier 14, Cryogenic air compressor 15, main heat exchanger 16, goes up tower 17, condenser/evaporator 18, following tower 19, subcooler 20, crude argon column 21-1, crude argon column 21-2, circulation liquid argon pump 22, pure argon column 23, liquid oxygen storage tank 24, liquid nitrogen storage 25, liquid argon storage tank 26:
1.3.1 purity nitrogen passage S25 → S26 that described air precooler 13 is provided with the enterprising raw air passage S21 → S22 that goes out down, the dirty nitrogen passage S23 → S24 that goes out on advancing down, goes out on advancing down;
1.3.2 be provided with in the described main heat exchanger 16 the enterprising raw air heat exchanger channels S18 → S29 that goes out down, the dirty nitrogen passage S30 → S23 that goes out on advancing down, the purity nitrogen passage S31 → S25 that goes out on advancing down and in press channel of nitrogen S32 → S17;
1.4 the order of connection of described nitrogen refrigerating circulatory device is: the ABC of S11 begins from middle pressure nitrogen, meet the middle pressure circulating nitrogen gas heat exchanger channels S5 → S6 in the liquefied natural gas heat exchanger 5, connect the circularly-supercharged machine 3 of low temperature nitrogen, connect expansion-supercharger 4, meet the cycle of higher pressure nitrogen heat exchanger channels S3 → S4 of liquefied natural gas heat exchanger 5, after interface S4, be divided into two-way; The road connects supercharging one decompressor 7, and another road meets the cycle of higher pressure nitrogen heat exchanger channels S4 → S7 in the cryogenic heat exchanger 6, after choke valve J1 and the first via are intersected in S10, is connected to gas-liquid separator 8 again; The top exit S12 of described gas-liquid separator meets the middle pressure circulating nitrogen gas heat exchanger channels S8 → S9 in the cryogenic heat exchanger 6, is intersected in nitrogen inlet S11 after meeting the middle pressure circulating nitrogen gas heat exchanger channels S12 → S13 in the aerial cooler 9 again; The outlet at bottom S20 of described gas-liquid separator divides two-way to go out, and one the tunnel is connected to the following tower S28 of air separation unit, the middle hydraulic fluid nitrogen heat exchanger channels S16 → S17 of another road in breather valve T3 is connected to air liquefier 10 through breather valve T2; After described natural gas basin 1 connects liquefied natural gas booster pump 2, meet the liquefied natural gas heat exchanger channels S1 → S2 in the liquefied natural gas heat exchanger 5.
1.5 the order of connection of described air-separating plant is: n1 begins from air intlet, connect air cleaner 11, connect air compressor 12, meet the enterprising raw air passage S21 → S22 that goes out down in the air precooler 13, connect molecular sieve purifier 14, again behind the raw air heat exchanger channels S14 → S15 in aerial cooler 9, connect Cryogenic air compressor 15 backs and divide two-way, one the tunnel meets the raw air heat exchanger channels S18 → S19 in the air liquefier 10, meet down tower S19 again, another road meets the enterprising raw air heat exchanger channels S18 → S29 that goes out down in the main heat exchanger 16, be connected to down tower S29 again: through connecting upward tower 17 behind the tower 19 down, crude argon column 21-1, crude argon column 21-2, pure argon column 23 is connected with circulation liquid argon pump 22 between described crude argon column 21-1 and the crude argon column 21-2, connect liquid oxygen storage tank 24 at last, liquid nitrogen storage 25, liquid argon storage tank 26.
When present embodiment uses:
(1) flow process of nitrogen circulation: when device starts, close breather valve T2, T4, open breather valve T1, T3.The nitrogen of 600KPa is drawn from the top S27 of the following tower 19 of air-separating plant, enter the nitrogen cooling cycle system through breather valve T1, through air liquefier 10 posterior nodal point S17, converge at the S11 place with the nitrogen that comes out through aerial cooler 9, enter liquefied natural gas heat exchanger 5 (S5 → S6) and liquefied natural gas heat exchange (S1 → S2), temperature is reduced to-110 ℃～-120 ℃, enter nitrogen supercharging machine 3 and be pressurized to 3000KPa～3500KPa, the supercharger 4 at decompressor is compressed to 3600KPa～200KPa again; Enter liquefied natural gas heat exchanger 5 again with liquefied natural gas heat exchange (S3 → S4), be cooled to-140 ℃～-142 ℃; Be divided into two-way: the one tunnel goes decompressor 7 to expand, and further lowers the temperature and produces part liquid, enters gas-liquid separator 8 and carries out gas-liquid separation; Another road is at cryogenic heat exchanger 6 (the nitrogen heat exchange that S4 → S7) and separator 8 come out (S8 → S9), after temperature further drops to about-160 ℃, (S7 → S10) also produce partly liquid also enters gas-liquid separator 8 and carries out gas-liquid separation to go choke valve J1 throttling expansion.The liquid nitrogen of separating (startup stage liquid nitrogen send S28 place, Xia Ta top back to through breather valve T2) is delivered to air liquefier 10 through breather valve T3, and (S16 → S17) and the Cryogenic air compressor 15 part air of coming carries out heat exchange, and (S18 → S19) also makes air liquefy at the S19 place.The nitrogen that separator 8 is separated is through its top exit S12, through cryogenic heat exchanger 6 (behind the S8 → S9), (S12 → S13) is with the raw air heat exchange that is come by molecular sieve purifier 14 sieves (S14 → S15), and make air themperature drop to-90 ℃～-100 ℃ to enter aerial cooler 9.With after the nitrogen after air liquefier 10 heat exchange meets at node S11, enter liquefied natural gas heat exchanger 5 (S5 → S6) at the nitrogen after aerial cooler 9 heat exchange; Begin repetition above-mentioned steps (after treating that nitrogen gas purity is qualified, closing breather valve T1, T2, T3) again, and do not stop circulation with this.
When nitrogen circulating system because of the gas leakage operating pressure during less than following tower operating pressure, pressure maintaining valve W1 opens automatically, carries out automatic tonifying Qi
The liquid nitrogen of liquid nitrogen storage (as be stored in) arranged under the condition in liquid nitrogen source, can directly open the liquid nitrogen that breather valve T2, T4 introduce in the storage tank and start, this moment, breather valve T1, T3 were closed condition.
Above-mentioned breather valve T1, T2, the effect of T3 are when air separation unit starts (when not having the liquid nitrogen source), the middle nitrogen of pressing is from following tower 19, the liquid nitrogen that produces is sent down tower 19 (with in-line analyzer monitoring LNG trace) back to, after the purity of central pressure nitrogen reaches requirement, just cuts off their contact; And when the normal operation of device, when the circulatory system of nitrogen needed tonifying Qi because of leakage, pressure maintaining valve W1 opened, and closed after supplying, and avoided air separation unit when normal operation, and LNG brings distillation system into; Breather valve T4 is the valve that connects between liquid nitrogen storage and the closed cryogenic cycles, and its effect is to start air separation unit with the liquid nitrogen in the liquid nitrogen storage, and anti-locking apparatus is brought LNG into distillation system when starting.
(2) flow process of air liquefaction separation: raw air is sucked by air compressor 12 through air cleaner 11, after being compressed to 180KPa～21OKPa, (((heat exchange of S23 → S24) also is cooled to 15 ℃～17 ℃ for S25 → S26) and purity nitrogen for S21 → S22) and returning polluted nitrogen to enter air precooler 13.Remove CO through molecular sieve purifier 14
2Behind moisture content, enter aerial cooler 9 (S14 → S15) and middle pressure nitrogen (S12 → S13) heat exchange again, be cooled to-90 ℃～-100 ℃, sucked by Cryogenic air compressor 15, after further boosting to 600KPa, be divided into two-way: the one tunnel removes air liquefier 10, and ((S16 → S17) and all liquefaction are delivered to S19 places in the middle of the following tower 19 of air-separating plant, tower 19 rectifying under participating at last in the liquid nitrogen heat exchange of S18 → S19) and kind of refrigeration cycle; Another road enters the main heat exchanger 16 of air-separating plant, and (((S31 → S25) heat exchange is sent down S29 place, tower 19 bottom to saturation state, participates in tower 19 rectifying down for S30 → S23) and purity nitrogen for S18 → S29) and the dirty nitrogen that backflows; After this, raw air following tower 19, on the process of rectifying in the tower 17, crude argon column 21-1,21-2, pure argon column 23, identical with traditional liquid air separation unit, produce space division product at last---liquid oxygen, liquid nitrogen, liquid argon, put into liquid oxygen storage tank 24, liquid nitrogen storage 25, liquid argon storage tank 26 respectively.
Embodiment two:
On the technical foundation of embodiment one, aerial cooler 9 and Cryogenic air compressor 15 are omitted, node S6 and S9 are merged into node S6; Node S14 and S18 are merged into node S14.
When present embodiment uses:
(1) flow process of the cold circulation of nitrogen: when device starts, close breather valve T2, T4, open breather valve T1, T3.The nitrogen of 600KPa is drawn from the top S27 of the following tower 19 of air-separating plant, enter the nitrogen cooling cycle system through breather valve T1, enter air liquefier 10 (S16 → S17) with from the raw air heat exchange of molecular sieve 4 (behind the S18 → S19), enter liquefied natural gas heat exchanger 5 (S5 → S6) again, (S1 → S2) obtains cold with the liquefied natural gas heat exchange, temperature is reduced to-120 ℃～-130 ℃, enter nitrogen supercharging machine 3 and be pressurized to 3000KPa～3500KPa, supercharger 4 at decompressor is compressed to 3600KPa～4200KPa again, enter liquefied natural gas heat exchanger 5 (S3 → S4) again with liquefied natural gas heat exchange (S1 → S2), be cooled to-140 ℃～-142 ℃, be divided into two-way: the one tunnel goes decompressor 7 to expand, further cooling and generation part liquid enter gas-liquid separator 8 and carry out gas-liquid separation; Another road is at cryogenic heat exchanger 6 (the nitrogen heat exchange that S4 → S7) and separator 8 come out (S8 → S9), after temperature further drops to about 160 ℃, (S7 → S10) also produces partly liquid to go choke valve J1 throttling expansion, also enter gas-liquid separator 8 and carry out gas-liquid separation, the liquid nitrogen of separating (startup stage liquid nitrogen send S28 place, Xia Ta top back to through breather valve T2) is delivered to air liquefier 10 through breather valve T3, and (S16 → S17) and the molecular sieve purifier 14 part air of coming carries out heat exchange, and (S18 → S19) also makes air liquefaction, send into down tower S19 place, participate in tower 19 rectifying down, the nitrogen that separator 8 is separated is through its top exit S12, through low temperature heat exchanger 6 (behind the S8 → S9), after converging in node S6 place with the middle pressure nitrogen of the heat exchange gas device 5 that goes out to liquefy, temperature becomes-120 ℃～-130 ℃, enter nitrogen supercharging machine 3 and be pressurized to 3000KPa～3500KPa, begin the repetition above-mentioned steps again (after treating that nitrogen gas purity is qualified, close breather valve T1, T2, T3, T4), and with this do not stop circulation.
When nitrogen circulating system because of the gas leakage operating pressure during less than following tower operating pressure, pressure maintaining valve W1 opens automatically, carries out automatic tonifying Qi
The liquid nitrogen of liquid nitrogen storage (as be stored in) arranged under the condition in liquid nitrogen source, can directly open the liquid nitrogen that breather valve T2, T4 introduce in the storage tank and start, this moment, breather valve T1, T3 were closed condition.
(2) implementing procedure of air-separating plant: raw air is through air cleaner 11, sucked by air compressor 12, be compressed to 600KPa～620KPa, (((heat exchange of S23 → S24) also is cooled to 13 ℃～17 ℃ for S25 → S26) and purity nitrogen for S21 → S22) and returning polluted nitrogen to enter air precooler 13.Remove CO through molecular sieve purifier 14
2Behind moisture content, be divided into two-way: the one tunnel removes air liquefier 10, and ((S16 → S17) heat exchange and all liquefaction delivered to S19 places in the middle of the following tower 19 of air separation unit, tower 19 rectifying under participating at last for S18 → S19) and liquid nitrogen; Another road enters the main heat exchanger 16 of air separation unit, and (((S30 → S23) heat exchange is sent down S29 place, tower 19 bottom to saturation temperature, goes to participate in down tower 19 rectifying for S31 → S25) and purity nitrogen for S18 → S29) and the dirty nitrogen that backflows.After this, raw air following tower 19, on the process of rectifying in the tower 17, crude argon column 21-1,21-2, pure argon column 23, identical with traditional liquid air separation unit, produce space division product at last---liquid oxygen, liquid nitrogen, liquid argon, put into liquid oxygen storage tank 24, liquid nitrogen storage 25, liquid argon storage tank 26 respectively.
The utility model not only can effectively reclaim the cold energy of liquefied natural gas, reduces operating cost and environmental pollution, and when producing liquid form product, can reduce power consumption and water consumption significantly, has bigger application and popularization value.
Claims (2)
1, a kind of air-separating plant that reclaims cold energy of liquefied natural gas, comprise with cold energy of liquefied natural gas and make nitrogen refrigerating circulatory device, the air liquefaction separation of precooling, the aerial cooler (9) that is used to connect nitrogen refrigerating circulatory device and air liquefaction separation and air liquefier (10), be used to start and normally move required one group of valve and connecting line, it is characterized in that:
1.1 press circulating nitrogen gas heat exchanger channels (S12 → S13) and raw air heat exchanger channels (S14 → S15), (S16 → S17) and the raw air heat exchanger channels (S18 → S19) of hydraulic fluid nitrogen heat exchanger channels in being provided with in the described air liquefier (10) in being provided with in the described aerial cooler (9);
1.2 described nitrogen refrigerating circulatory device comprises liquefied natural gas basin (1), liquefied natural gas booster pump (2), the circularly-supercharged machine of low temperature nitrogen (3), expansion-supercharger (4), liquefied natural gas heat exchanger (5), cryogenic heat exchanger (6), supercharging-decompressor (7), choke valve (J1), gas-liquid separator (8) and connecting line thereof;
1.2.1 be provided with liquefied natural gas heat exchanger channels (S1 → S2), cycle of higher pressure nitrogen heat exchanger channels (S3 → S4) and middle pressure circulating nitrogen gas heat exchanger channels (S5 → S6) in the described liquefied natural gas heat exchanger (5);
1.2.2 be provided with cycle of higher pressure nitrogen heat exchanger channels (S4 → S7) and middle pressure circulating nitrogen gas heat exchanger channels (S8 → S9) in the described cryogenic heat exchanger (6);
1.3 described air liquefaction separation comprises air cleaner (11), air compressor (12), air precooler (13), molecular sieve purifier (14), Cryogenic air compressor (15), main heat exchanger (16), goes up tower (17), condenser/evaporator (18), following tower (19), subcooler (20), crude argon column (21-1), crude argon column (21-2), circulation liquid argon pump (22), pure argon column (23), liquid oxygen storage tank (24), liquid nitrogen storage (25), liquid argon storage tank (26);
1.3.1 described air precooler (13) is provided with the enterprising raw air passage that goes out down (the dirty nitrogen passage of S21 → go out on advancing S22), down (the purity nitrogen passage of S23 → go out on advancing S24), down (S25 → S26);
1.3.2 be provided with in the described main heat exchanger (16) the enterprising raw air heat exchanger channels that goes out down (the dirty nitrogen passage of S18 → go out on advancing S29), down (the purity nitrogen passage of S30 → go out on advancing S23), down (S31 → S25) and in press channel of nitrogen (S32 → S17);
1.4 the order of connection of described nitrogen refrigerating circulatory device is:, connect the liquefaction sky from middle pressure nitrogen inlet (S11) beginning
Middle pressure circulating nitrogen gas heat exchanger channels in the right gas heat exchanger (5) (S5 → S6), connect the circularly-supercharged machine of low temperature nitrogen (3), connect expansion-supercharger (4), (S3 → S4), (S4) is divided into two-way afterwards at interface to connect the cycle of higher pressure nitrogen heat exchanger channels of liquefied natural gas heat exchanger (5); One the tunnel connects supercharging-decompressor (7), and another road meets the cycle of higher pressure nitrogen heat exchanger channels (S4 → S7), after the choke valve (J1) and the first via are intersected in (S10), be connected to gas-liquid separator (8) again in the cryogenic heat exchanger (6); The top exit of described gas-liquid separator (S12) connects middle pressure circulating nitrogen gas heat exchanger channels in the cryogenic heat exchanger (6), and (S8 → S9) connects middle pressure circulating nitrogen gas heat exchanger channels in the aerial cooler (9) again and (is intersected in nitrogen inlet (S11) behind the S12 → S13); The outlet at bottom of described gas-liquid separator (S20) divides two-way to go out, and one the tunnel is connected to the following tower S28 of air separation unit through breather valve (T2), and the middle hydraulic fluid nitrogen heat exchanger channels of another road in breather valve (T3) is connected to air liquefier (10) (S16 → S17); After described natural gas basin (1) connects liquefied natural gas booster pump (2), meet liquefied natural gas heat exchanger channels in the liquefied natural gas heat exchanger (5) (S1 → S2);
1.5 the order of connection of described air-separating plant is: begin from air intlet (n1), connect air cleaner (11), connect air compressor (12), meet (the S21 → S22) of the enterprising raw air passage that goes out down in the air precooler (13), connect molecular sieve purifier (14), raw air heat exchanger channels in aerial cooler (9) is (behind the S14 → S15) again, connect Cryogenic air compressor (15) back and divide two-way, one the tunnel meets raw air heat exchanger channels in the air liquefier (10) (S18 → S19), connect down tower (S19) again, another road meets the enterprising raw air heat exchanger channels (S18 → S29), be connected to down tower (S29) again that goes out down in the main heat exchanger (16); Through connecting upward tower (17), crude argon column (21-1) behind the tower (19) down, crude argon column (21-2), pure argon column (23), be connected with circulation liquid argon pump (22) between described crude argon column (21-1) and the crude argon column (21-2), connect liquid oxygen storage tank (24), liquid nitrogen storage (25), liquid argon storage tank (26) at last.
2, the air-separating plant of recovery cold energy of liquefied natural gas according to claim 1, (S32 → S17) is provided with pressure maintaining valve (W1) to the channel of nitrogen that it is characterized in that being connected between main heat exchanger (16) and the air liquefier (10).
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| Application Number | Priority Date | Filing Date | Title |
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| CNU2005202003068U CN2766203Y (en) | 2005-04-15 | 2005-04-15 | Air separator for recovering cold energy of liquefied natural gas |
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| CNU2005202003068U CN2766203Y (en) | 2005-04-15 | 2005-04-15 | Air separator for recovering cold energy of liquefied natural gas |
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| CN101846436A (en) * | 2010-05-27 | 2010-09-29 | 中国海洋石油总公司 | Full-liquid air separation device using cold energy of liquefied natural gas (LNG) |
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| CN103759499B (en) * | 2014-01-13 | 2016-05-25 | 浙江海天气体有限公司 | A kind of super low energy consumption nitrogen-making device |
| CN103759499A (en) * | 2014-01-13 | 2014-04-30 | 浙江海天气体有限公司 | Ultralow-energy-consumption nitrogen making device |
| CN107429967B (en) * | 2015-03-17 | 2020-03-10 | 西亚德汽车***股份公司 | Plant for liquefying nitrogen using recovery of cold energy obtained from the evaporation of liquefied natural gas |
| CN107429967A (en) * | 2015-03-17 | 2017-12-01 | 西亚德汽车***股份公司 | Carry out the equipment of liquid nitrogen using the cold energy recovery obtained from the evaporation of liquefied natural gas |
| CN108072235A (en) * | 2016-11-17 | 2018-05-25 | 北大方正集团有限公司 | Space division system |
| CN110319651A (en) * | 2018-03-29 | 2019-10-11 | 舒伟 | A kind of natural gas gathering system and collection transportation method based on cold energy circulation |
| CN109855389A (en) * | 2019-01-04 | 2019-06-07 | 曹建喜 | A method of liquid oxygen liquid nitrogen is produced using LNG cold energy and single tower distillation technique |
| CN109855389B (en) * | 2019-01-04 | 2020-11-13 | 曹建喜 | Method for producing liquid oxygen and liquid nitrogen by using LNG cold energy and single-tower rectification process |
| CN109595461A (en) * | 2019-01-15 | 2019-04-09 | 江苏科技大学 | A kind of LNG is regasified and liquid air preparation system and working method |
| CN109595461B (en) * | 2019-01-15 | 2021-05-04 | 江苏科技大学 | LNG regasification and liquid air preparation system and working method |
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