CN109140903A - A kind of space division system and air separating method using cold energy of liquefied natural gas - Google Patents

A kind of space division system and air separating method using cold energy of liquefied natural gas Download PDF

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CN109140903A
CN109140903A CN201810973812.2A CN201810973812A CN109140903A CN 109140903 A CN109140903 A CN 109140903A CN 201810973812 A CN201810973812 A CN 201810973812A CN 109140903 A CN109140903 A CN 109140903A
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nitrogen
heat exchanger
liquid
lng
gas
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CN109140903B (en
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邢仁钊
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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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • 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
    • 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
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • 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
    • F25J3/04151—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
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • 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
    • 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
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • 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
    • 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
    • F25J3/04272—The cryogenic component does not participate in the fractionation and being liquefied hydrocarbons and comprising means for reducing the risk of pollution of hydrocarbons into the air fractionation
    • 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
    • F25J3/04333—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
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F25J5/007—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger combined with mass exchange, i.e. in a so-called dephlegmator
    • 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
    • F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
    • 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
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/04—Compressor cooling arrangement, e.g. inter- or after-stage cooling or condensate removal
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • 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
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/42—One fluid being nitrogen
    • 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
    • F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
    • F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention discloses a kind of space division systems and air separating method using cold energy of liquefied natural gas.It includes air gas separation unit, LNG cold energy use unit and ethylene glycol solution circulating cooling unit；The production energy consumption of LNG cold energy space division system is greatly reduced in the new technological process organizational form that low-temperature circulating nitrogen compressor is replaced by using circulating liquid nitrogen pump, and oxygen, Argon recovery rate are high, and for product nitrogen gas liquefied fraction up to 100%, surcharge is high；Cold mode can be also mended by liquid nitrogen reflux and matches the variation of LNG cooling capacity, and few to LNG receiving station technical requirements, versatility is stronger；The present invention, which is realized, reduces by 40% or more than existing LNG cold energy spatial division technology comprehensive energy consumption, and specific energy consumption reduces by 60% or more beneficial effect, and extreme underproduction operating condition specific energy consumption is still below the prior art, and cost advantage is fairly obvious.

Description

A kind of space division system and air separating method using cold energy of liquefied natural gas
Technical field
The present invention relates to a kind of air separating method, in particular to a kind of air separation side using cold energy of liquefied natural gas Method.
Background technique
Natural gas is as one of chemical energy source, because of its huge reserves and low pollution, be incrementally raised for and coal, stone Main energy sources pillar after oil, has broad application prospects.The trade form of natural gas mainly has pipeline and LNG (liquefied natural gas) transport, LNG need to gasify from liquefaction to room temperature, gasify before entering natural gas user pipe network Journey will discharge huge cooling capacity.Air-separating plant can be significantly reduced power consumption, increase by making full use of the gasification cold energy of LNG The output of liquid feeding body, improves competitiveness of the product in market sale, and economic benefit is fairly obvious.But since space division system is Oxygen concentration area, natural gas are extremely sensitive harmful substances as hydrocarbon.Therefore, usually to the utilization of LNG cold energy Cold energy is transmitted using intermediate medium, LNG is avoided to contact with the direct of space division system.Domestic and international LNG cold energy air separation unit is made a general survey of, it is general Store-through is excessively complicated in its process organization, and energy consumption is higher, implements to be not easy, and operation control is inconvenient or security reliability is not good enough existing As.For example multiple compressors, more expanding machines, knockout drums etc. are used, heat exchanger channel is more, and especially LNG is high pressure, heat exchange Device channel is more, and cost is caused to sharply increase.Furthermore process organization is complicated, and the more region of the electrical components such as valve, measurement point needs It is explosion-proof, hidden danger is brought for the safety of device.
Chinese patent application specification CN 101571340A discloses a kind of space division system using cold energy of liquefied natural gas System, the patent use the circulation nitrogen compressor of three sections of low temperature air inlets, and using glycol-cooled system, but the acquisition of liquid oxygen product is main It is to throttle to exchange heat with it to low pressure with the high pressure overfreezing liquid nitrogen in LNG- nitrogen heat exchanger by low oxygen, and recycle high-pressure liquid nitrogen One of the cold source of supercooling be the low pressure liquid nitrogen of throttling, i.e., one section of inlet flow rate is larger in circulation low temperature nitrogen compressor, causes Low temperature nitrogen compressor shaft power is higher.
Chinese patent application specification CN 101532768A discloses a kind of space division for efficiently utilizing cold energy of liquefied natural gas System, the patent a part of the embodiment use liquid expander and replace throttle valve, expand high-pressure liquid nitrogen, but cooling capacity transfer medium Circulating nitrogen gas drives by low-temperature circulating nitrogen compressor, circulating nitrogen gas is compressed to supercritical pressure, energy consumption ratio is pumped using liquid Contracting liquid nitrogen is higher by decades of times.And there are a large amount of high pure nitrogens to diffuse because that can not liquefy, cause the synthesis specific energy consumption of system into one Step increases.
For this reason, it may be necessary to develop the space division system using cold energy of liquefied natural gas for providing and can eliminating drawbacks described above.
Summary of the invention
It is an object of the invention to overcome the deficiencies of the prior art and provide a kind of versatile, liquefied natural gas cool is utilized The space division system of energy, the system organically combine the cryogenic cold energy for being pressurized to authorized pressure LNG with air gas separation unit, Take full advantage of the cold energy of LNG.
The present invention also provides a kind of space division systems using cold energy of liquefied natural gas to carry out air separating method, i.e., will The cryogenic cold energy of LNG is used to produce liquid space division product and interior compressed product gas, to reduce liquid space division product and interior compression The unit power consumption of gas products, while LNG heating of gasifying in space division system being made to reach the defeated temperature of pipe of requirement.
To achieve the above object the technical scheme adopted by the invention is that:
A kind of space division system using cold energy of liquefied natural gas, it is characterised in that: including air gas separation unit, LNG cold energy use Unit and ethylene glycol solution circulating cooling unit；
The ethylene glycol solution circulating cooling unit includes LNG- ethylene glycol heat exchanger 12 and ethylene glycol solution circulating pump 15；
The LNG cold energy use unit is swollen comprising circulating liquid nitrogen pump 9, LNG- nitrogen heat exchanger 11, gas-liquid separator 10, liquid pressurization Swollen machine 13 and vent muffler 17；
The air gas separation unit include self-cleaning air filter 1, air compressor 2, molecular sieve 3, regeneration hot-air heater 14, Main heat exchanger 4, liquefaction heat exchanger 5, rectifying column and vent muffler 16, rectifying column include lower tower 6, main condenser evaporator 7 and on 8 three parts of tower.
In above-mentioned air gas separation unit, the outlet of self-cleaning air filter 1 and 2 entrance phase of air compressor Even；3 entrance of molecular sieve is exported with air compressor machine 2 and vent muffler 16 is respectively connected with；Molecular sieve 3 outlet respectively with main heat exchanger 4 It is connected with regeneration hot-air heater 14；
4 hot end of main heat exchanger and cold end have three strands, and hot end is hot with the outlet of molecular sieve 3, LNG- nitrogen heat exchanger 11 respectively End is connected with regeneration hot-air heater 14；Cold end pumps 9 with a hot end of liquefaction heat exchanger 5 and a cold end, circulating liquid nitrogen respectively Outlet be connected；
5 hot end of liquefaction heat exchanger and cold end have six strands；Cold end respectively with 4 one cold ends of main heat exchanger, 8 top of upper tower It is connected with top, 6 top of lower tower, 10 top of gas-liquid separator with top；Hot end respectively with lower 6 bottom and top of tower, main heat exchange One cold end of device 4, a hot end of LNG- nitrogen heat exchanger 11 are connected with the pressurization end entrance of liquid booster expansion machine 13；
The top of the lower tower 6 be equipped with two groups of outlets and entrance, wherein one group respectively with the hot end of main condenser evaporator 7 and cold end It is connected, another group is connected with the hot end of liquefaction heat exchanger 5 and cold end respectively；Bottom inlet is connected with 5 hot end of liquefaction heat exchanger, bottom Portion outlet is connected through throttle valve with upper 8 top of tower；
Be connected at the top of 7 entrance of main condenser evaporator and lower tower 6, outlet is divided into three strands, respectively with 6 top of lower tower, product Liquid oxygen storage tank and through being connected at the top of throttle valve and upper tower 8；
The outlet of upper tower 8 is divided into three strands, is that top first outlet is connected with nitrogen products storage tank respectively, top second outlet It is connected respectively with two bursts of cold ends of liquefaction heat exchanger 5 with upper outlet；Top and top two entrances are evaporated with main condenser respectively Device 7 is connected with lower 6 bottom of tower.
For continuous uninterrupted use, it is two that the molecular sieve 3, which is divided to, is used alternatingly, one regeneration of a purifying.Purifying The entrance at end is connected with the outlet of air compressor machine 2, and the outlet for purifying end is connected with 4 hot end of main heat exchanger；The entrance caused trouble again and regeneration The outlet of hot-air heater 14 is connected, then the outlet caused trouble is connected with vent muffler 16.
In the ethylene glycol solution circulating cooling unit, 12 hot end of LNG- ethylene glycol heat exchanger and cold end have two Stock, two stocks of cold end are not connected with cryogenic natural gas pipeline and 2 interstage cooler of air compressor machine and aftercooler entrance, hot end It is connected respectively with natural gas line and the outlet of ethylene glycol solution circulating pump 15；
15 entrance of ethylene glycol solution circulating pump and 2 interstage cooler of air compressor machine are connected with aftercooler outlet, outlet with 12 hot end of LNG- ethylene glycol heat exchanger is connected；By reduce air compressor machine 2 two, three-level inlet temperature and molecular sieve intake air temperature, Achieve the effect that reduce air compressor machine energy consumption and molecular sieve absorption resistance.
In the LNG cold energy use unit, the circulating liquid nitrogen pumps 9 entrances and is connected with 10 bottom of gas-liquid separator, exports It is connected with 4 cold end of main heat exchanger；The mode that compressed gas is replaced by using compressed liquid uses liquid nitrogen pump generation that is, in equipment For low temperature nitrogen compressor, achieve the effect that energy consumption is greatly reduced.
10 top exit of gas-liquid separator is connected with 5 two bursts of cold ends of liquefaction heat exchanger respectively with upper entrance, top Another entrance is connected with liquid nitrogen product storage tank, and outlet at bottom pumps 9 entrances, nitrogen products storage tank and LNG- with circulating liquid nitrogen respectively Nitrogen heat exchanger 11 is connected；Centre entrance is connected with the outlet of 13 expanding end of liquid booster expansion machine；
In order to improve Nitrogen Headspace rate, the release waste of space division nitrogen product is reduced, is replaced using the liquid booster expansion machine of liquid nitrogen Liquid nitrogen throttle valve, the ability for making system have liquefaction all over products nitrogen.The liquid booster expansion machine 13 divide for pressurized end and Expanding end, the pressurization end entrance are connected with 5 two hot ends of liquefaction heat exchanger, and outlet is connected with 11 hot end of LNG- nitrogen heat exchanger； The expansion end entrance is connected with 11 cold end of LNG- nitrogen heat exchanger, and outlet is connected with gas-liquid separator 10；
11 cold end of LNG- nitrogen heat exchanger have five strands, hot end have four strands, cold end respectively with LNG pipeline, 5 heat of liquefaction heat exchanger End, liquid booster expansion machine 13 expand end entrance, LNG- ethylene glycol heat exchanger (12) is connected with 10 bottom of gas-liquid separator；Hot end It is connected respectively with natural gas line, the outlet of 13 pressurized end of liquid booster expansion machine, 4 hot end of main heat exchanger and vent muffler 17.
It is described in order to improve the adaptability for utilizing cold energy of liquefied natural gas space division system to change cold source LNG cooling capacity One heat exchanger channels is arranged in LNG- nitrogen heat exchanger 11, and both ends are connected with gas-liquid separator 10 and vent muffler 17 respectively, be It opens and uses when LNG cold energy deficiency；Heat exchange gas channel middle extract out one 604, with adjust input LNG- ethylene glycol heat exchange The cooling capacity of device 12.
In order to facilitate starting whole system, one pipeline being connected with nitrogen products tank is arranged in the gas-liquid separator 10 216, it is used in space division system starting.
Multiple logistics phase transformations influence heat exchange efficiency, the main heat exchanger 4, liquefaction heat exchanger 5, the heat exchange of LNG- nitrogen in order to prevent What device 11 was formed by individual one or by multiple points of heat exchangers, it avoids that Temperature cross-over occurs in heat exchanger.
The present invention also provides a kind of methods that the space division system using cold energy of liquefied natural gas carries out air separation, including Following steps:
A) raw air compresses after self-cleaning strainer 1 removes most of solid impurity into air compressor 2, by dividing Sub- screen system 3 obtains pure air 103 after removing the impurity such as water removal, hydrocarbon；
B) pure air 103 is in main heat exchanger 4 by extracting out with upper 8 top of tower and providing cooling capacity simultaneously in liquefaction heat exchanger 5 The dirty nitrogen 402 and cycle of higher pressure liquid nitrogen 501 of preliminary re-heat exchange heat and are cooled and liquefy；The complete re-heat in main heat exchanger Dirty nitrogen 403 connects purification system 3 and does regeneration gas and cold blowing gas；
C) air 104 after liquefying provides cooling capacity in liquefaction heat exchanger 5 for liquefaction pressure nitrogen 205 and 208, and re-heat is Gas-liquid mixed air 105, which enters in rectifying tower system, is separated into discharge logistics, and the discharge logistics includes obtaining at the top of upper tower 7 Pure nitrogen gas 202 and liquid nitrogen product 218, the dirty nitrogen 401 that is obtained from upper 7 top of tower, the liquid oxygen 301 obtained from upper tower bottom；
D) raw air 105 obtains oxygen-enriched liquid air 106 in lower 6 bottom of tower in lower tower 6 after initial gross separation, at lower 6 top of tower Medium pressure nitrogen gas is obtained, medium pressure nitrogen gas enters main condenser evaporator 7, liquid nitrogen is condensed by the liquid oxygen of upper 8 bottom of tower, the one of the liquid nitrogen Part sends lower tower 6 back to maintain the rectifying operating condition of lower tower 6, and the throttling of another part liquid nitrogen 201 is sent at the top of upper tower 8 and participates in rectifying； In addition it extracts one pressure nitrogen gas 208 out and enters liquefaction heat exchanger 5, lower tower 6 is returned after being liquefied and does phegma；Oxygen-enriched liquid air 106 It is sent into after throttling in the middle part of upper tower 8 and participates in the rectifying of upper tower 8；
E) it is sent into the gas oxygen progress rectifying again that liquid nitrogen 201, oxygen-enriched liquid air 106 and the main condenser evaporator 7 of upper tower evaporate, from Obtain low-pressure nitrogen 202 and liquid nitrogen 218 at the top of upper tower 8, obtain dirty nitrogen 401 from upper 8 top of tower, main condenser evaporator 7 it is upper Portion is connected to upper 8 bottom of tower, is obtained liquid oxygen in upper 8 bottom of tower, is extracted unvaporized liquid oxygen 301 out from main condenser evaporator 7, send It is used as product liquid oxygen out；The dirty nitrogen 401 obtained from upper 8 top of tower re-heat in liquefaction heat exchanger 5 and main heat exchanger 4 heats up out It is divided into two-way after air gas separation unit, dirty nitrogen goes type air purifier 3 to make regeneration gas through regenerating hot-air heater 16 all the way, all the way Vent muffler is gone to be vented as dirty nitrogen is vented；If space division has ar system, Argon fraction is obtained in the middle part of upper tower, Argon fraction is sent Enter argon producing system and produce product liquid argon, which be not repeated herein known to industry technical staff；
F) a part of liquid nitrogen 213 obtained in gas-liquid separator 10 is pressurised into supercritical pressure liquid nitrogen into circulating liquid nitrogen pump 9 501 and enter 4 re-heat of main heat exchanger be room temperature after, overcritical liquid nitrogen is cooled to by high pressure LNG602 into LNG- nitrogen heat exchanger 11 503, obtain LNG cold energy；Enter 13 expanding end of liquid booster expansion machine after liquefaction and is expanded to low-pressure gas-liquid mixing nitrogen 210, into Enter gas-liquid separator 10 and is separated into nitrogen 211 and liquid nitrogen.The pure nitrogen gas 202 extracted out at the top of upper tower 8 is changed with nitrogen 211 into liquefaction Hot device 5 provides cooling capacity, and nitrogen 203 is mixed into after re-heat and enters 13 pressurized end boil down to low-pressure nitrogen of liquid booster expansion machine 204, the further cooling of liquefaction heat exchanger 5 is entered back into after being cooled into LNG- nitrogen heat exchanger 11 and is liquefied as liquid nitrogen 206, throttling Enter gas-liquid separator 10 afterwards, is mixed into liquid nitrogen 212 with the liquid nitrogen separated after expansion；
G) tri- tunnel 212 Fen Wei of liquid nitrogen in gas-liquid separator 10, circulating liquid nitrogen 213, nitrogen products 217 and the cold liquid nitrogen 214 of benefit；It follows 213 flow of ring liquid nitrogen immobilizes, and when LNG601 meets requirement of system design, mending cold 214 flow of liquid nitrogen is 0, works as LNG601 When flow is higher than design temperature or two kinds of situations while occurring lower than design discharge or temperature, product liquid is reduced by actual conditions 217 flow of nitrogen increases and mends cold 214 flow of liquid nitrogen, to maintain system stable operation；Under extreme case, also it can be used in storage tank Liquid nitrogen is mended cold；
H) LNG601 gasifies after exchanging heat to go out the natural gas 604 and 605 of LNG- nitrogen heat exchanger 11, middle 604 temperature of pumping natural gas It is still below 0 degree, is exchanged heat in ethylene glycol heat exchanger 12 after mixing LNG603 with glycol water 701, LNG603 and day are obtained Cooling medium of the glycol water 703 of 604 cold energy of right gas as air compressor machine 2 interstage cooler and aftercooler, heat exchange Glycol water 702 afterwards pressurizes through ethylene glycol solution circulating pump 15, returns ethylene glycol heat exchanger 12 and carries out cycle heat exchange, LNG603 and natural gas 604 are warming up to normal-temperature natural-gas 606 and mix feeding gas distributing system 607 with natural gas 605.
Natural gas leakage enters air gas separation unit threat production safety, above-mentioned supercritical steam cycle nitrogen 502 in order to prevent Pressure is higher than LNG601, and it is smaller to the leakage of nitrogen 502 possibility that LNG601 occurs；Report is provided on 205 pipeline of nitrogen Alert chain hydrocarbon detector.In case of pollution, can emergency cut-off liquid nitrogen 217, prevent liquid nitrogen in pollution storage tank.
Beneficial effects of the present invention:
In the present invention, it is pumped contracting liquid nitrogen using circulating liquid nitrogen, as driving air gas separation unit and LNG cold energy use unit Between cooling capacity transfer medium method, compared with low-temperature circulating nitrogen compressor in the prior art, the energy consumption and equipment of liquid nitrogen pump Investment can reduce by 90% or more；In addition, low-temperature circulating nitrogen compressor is more than the acting irreversible loss that circulating liquid nitrogen pumps, also The dosage of LNG can substantially be raised；Meanwhile low-temperature circulating nitrogen compressor belongs to Special Compressor, operation difficulty and upkeep cost It is higher；By the present invention in that replacing the new technological process organizational form of low-temperature circulating nitrogen compressor with circulating liquid nitrogen pump, solve existing Have for driving a series of problems, such as equipment energy consumption of circulating nitrogen gas is high, investment is big, complicated for operation, maintenance is expensive in technology, it is real It is strong with property.
In the present invention, using liquid expander expansion by LNG supercritical pressure liquid nitrogen after cooling, and meanwhile it is defeated to pressurized end Not liquefied nitrogen liquefies for further cooling throttling and provides condition in function compressibility out, and liquid booster expansion machine is abundant While using high-pressure liquid nitrogen pressure energy, the liquefied fraction of product nitrogen gas greatly improved；Compared with liquid throttle valve, although liquid Booster expansion machine has the disadvantages such as equipment investment is high, takes up a large area, but is intended to reach identical liquid yield under the same conditions, makes It is also needed to increase a low temperature nitrogen compressor with liquid throttle valve, also will increase system energy consumption about 14% while increasing investment； By the present invention in that replacing liquid throttle valve with liquid booster expansion machine, solve the super-pressure liquid nitrogen bulbs of pressure in the prior art The problem of capable of wasting, it further reduced production energy consumption.
In the present invention, it is provided with one heat exchanger channels, nitrogen products is allow to flow through LNG- nitrogen heat exchanger released cold quantity Part LNG cold source is substituted, the resistance that system fluctuates LNG cooling capacity greatly improved.Outside LNG receiving station displacement generally fluctuate compared with Greatly, and flowed fluctuation also will affect LNG temperature, and LNG stream amount and temperature change can seriously affect the normal fortune of cold energy space division Job produces；Production cost of the present invention is low, when LNG cold source is undesirable, can use the method for replacing LNG with nitrogen products, really Protect space division system stable operation；The liquid nitrogen product that LNG cold energy use unit of the present invention extracts all flows through LNG- nitrogen heat exchanger gas Under the operating condition of change, the average production cost of liquid product is still lower than the production cost of the prior art, has very strong competitiveness.This Invention solves cold energy space division in the prior art and connects to LNG by using the mode of nitrogen products reflux LNG cold energy use unit The high problem of outer defeated LNG cold energy quality dependency degree of standing is received, it is more adaptable, it produces more stable.
Above-mentioned technical proposal of the present invention for details see attached table with domestic LNG cold energy space division main performance can be seen that this from subordinate list Real invention performance is better than advanced international level, and energy-saving effect is very significant.
Technical indicator comparative analysis:
Note: standard condition is that 214 pipelines mend the operating condition that cold liquid nitrogen flow is zero；
Minimum operating condition is the operating condition that 217 duct products liquid nitrogen flows are zero；
It needs to mend cold operating condition using liquid nitrogen in storage tank, is extreme case, does not list here.
Detailed description of the invention
Fig. 1 is the working principle of the invention figure.
In figure: 1- self-cleaning air filter, 2- air presses, 3- molecular sieve, 4- main heat exchanger, 5- liquefaction heat exchanger, Tower under 6-, 7- main condenser evaporator, the upper tower of 8-, 9- circulating liquid nitrogen pump, 10- gas-liquid separator, 11-LNG- nitrogen heat exchanger, 12- LNG- ethylene glycol heat exchanger, 13- liquid booster expansion machine, 14- regenerate hot-air heater, 15- ethylene glycol solution circulating pump, and 16- is put Empty muffler, 17- vent muffler.
101- primary filtration air, 102- compressed air, the pure compressed air of 103-, 104- liquid compressed air, 105- Gas-liquid mixed compressed air, 106- oxygen-enriched liquid air, the cold liquid nitrogen of 201- master, 202/203- nitrogen, 204/205- medium pressure nitrogen gas, 206- Middle hydraulic fluid nitrogen, 207- liquid nitrogen, tower nitrogen under 208-, the auxiliary cold liquid nitrogen of 209-, 210- gas-liquid mixed nitrogen, 211- nitrogen, 212/ 213- liquid nitrogen, the cold liquid nitrogen of 214- benefit, 215- liquid nitrogen, 216- starting liquid nitrogen, 217/218- nitrogen products, 301- product liquid oxygen, Dirt nitrogen, 403- room temperature dirt nitrogen, the overcritical liquid nitrogen of 501-, the overcritical nitrogen at room of 502-, the overcritical liquid of 503- Nitrogen, 601/602/603-LNG, 604- low temperature NG, 605/606/607- room temperature NG, 701/702- high temperature glycol aqueous solution, 703- low-temperature glycol aqueous solution.
Specific embodiment
In order to clarify the technical characteristics of the invention, below by specific embodiment, and in conjunction with attached drawing, to the present invention It is described further.
Embodiment one:
A kind of space division system using cold energy of liquefied natural gas, including air gas separation unit, LNG cold energy use unit and ethylene glycol Solution circulating cooling unit；
The ethylene glycol solution circulating cooling unit includes LNG- ethylene glycol heat exchanger 12 and ethylene glycol solution circulating pump 15；
The LNG cold energy use unit is swollen comprising circulating liquid nitrogen pump 9, LNG- nitrogen heat exchanger 11, gas-liquid separator 10, liquid pressurization Swollen machine 13 and vent muffler 17；
The air gas separation unit include self-cleaning air filter 1, air compressor 2, molecular sieve 3, regeneration hot-air heater 14, Main heat exchanger 4, liquefaction heat exchanger 5, rectifying column and vent muffler 16, rectifying column include lower tower 6, main condenser evaporator 7 and on 8 three parts of tower.
In the air gas separation unit:
The outlet of self-cleaning air filter 1 is connected with 2 entrance of air compressor；3 entrance of molecular sieve and air compressor machine 2 export It is connected with vent muffler 16；The outlet of molecular sieve 3 is connected with main heat exchanger 4 and regeneration hot-air heater 14；
4 hot end of main heat exchanger and cold end have three strands, and hot end is hot with the outlet of molecular sieve 3, LNG- nitrogen heat exchanger 11 respectively End is connected with regeneration hot-air heater 14；Cold end pumps 9 with a hot end of liquefaction heat exchanger 5 and a cold end, circulating liquid nitrogen respectively Outlet be connected；
5 hot end of liquefaction heat exchanger and cold end have six strands；Cold end respectively with 4 one cold ends of main heat exchanger, 8 top of upper tower It is connected with top, 6 top of lower tower, 10 top of gas-liquid separator with top；Hot end respectively with lower 6 bottom and top of tower, main heat exchange One cold end of device 4, a hot end of LNG- nitrogen heat exchanger 11 are connected with the pressurization end entrance of liquid booster expansion machine 13；
The top of the lower tower 6 be equipped with two groups of outlets and entrance, wherein one group respectively with the hot end of main condenser evaporator 7 and cold end It is connected, another group is connected with the hot end of liquefaction heat exchanger 5 and cold end respectively；Bottom inlet is connected with 5 hot end of liquefaction heat exchanger, bottom Portion outlet is connected through throttle valve with upper 8 top of tower；
Be connected at the top of 7 entrance of main condenser evaporator and lower tower 6, outlet is divided into three strands, respectively with 6 top of lower tower, product Liquid oxygen storage tank and through being connected at the top of throttle valve and upper tower 8；
The outlet of upper tower 8 is divided into three strands, is that top first outlet is connected with nitrogen products storage tank respectively, top second outlet It is connected respectively with two bursts of cold ends of liquefaction heat exchanger 5 with upper outlet；Top and top two entrances are evaporated with main condenser respectively Device 7 is connected with lower 6 bottom of tower.
It is two that the molecular sieve 3, which is divided to, is used alternatingly, one regeneration of a purifying；The entrance at purifying end goes out with air compressor machine 2 Mouth is connected, and the outlet for purifying end is connected with the hot end of main heat exchanger 4；The entrance caused trouble again exports phase with regeneration hot-air heater 14 Even, then the outlet caused trouble is connected with vent muffler 16.
In the ethylene glycol solution circulating cooling unit:
12 hot end of LNG- ethylene glycol heat exchanger and cold end have two strands, two stocks of cold end not with cryogenic natural gas pipeline and Two interstage coolers of air compressor machine 2 are connected with aftercooler entrance, two stocks in hot end not with natural gas line and second two The outlet of alcoholic solution circulating pump 15 is connected；
15 entrance of ethylene glycol solution circulating pump and 2 interstage cooler of air compressor machine and aftercooler outlet are connected, outlet and 12 hot end of LNG- ethylene glycol heat exchanger is connected.
In the LNG cold energy use unit:
The circulating liquid nitrogen pumps 9 entrances and is connected with 10 bottom of gas-liquid separator, and outlet is connected with 4 cold end of main heat exchanger；
10 top exit of gas-liquid separator is connected with 5 two bursts of cold ends of liquefaction heat exchanger respectively with upper entrance, and top is another A entrance is connected with liquid nitrogen product storage tank, and outlet at bottom pumps 9 entrances, nitrogen products storage tank and LNG- nitrogen with circulating liquid nitrogen respectively and changes Hot device 11 is connected；Centre entrance is connected with the outlet of 13 expanding end of liquid booster expansion machine；
The liquid booster expansion machine 13 divides for pressurized end and expanding end, the pressurization end entrance and 5 two heat of liquefaction heat exchanger End is connected, and outlet is connected with 11 hot end of LNG- nitrogen heat exchanger；The expansion end entrance is connected with 11 cold end of LNG- nitrogen heat exchanger, out Mouth is connected with gas-liquid separator 10；
11 cold end of LNG- nitrogen heat exchanger have five strands, hot end have four strands, cold end respectively with LNG pipeline, 5 heat of liquefaction heat exchanger End, liquid booster expansion machine 13 expand end entrance, LNG- ethylene glycol heat exchanger 12 is connected with 10 bottom of gas-liquid separator；Hot end point It is not connected with natural gas line, the outlet of 13 pressurized end of liquid booster expansion machine, 4 hot end of main heat exchanger and vent muffler 17.
The LNG- nitrogen heat exchanger 11 is arranged one heat exchanger channels, both ends respectively with gas-liquid separator 10 and vent muffler 17 are connected, and use to open in LNG cold energy deficiency；Heat exchange gas channel middle extract out one 604, with adjust input LNG- The cooling capacity of ethylene glycol heat exchanger 12.
One pipeline 216 being connected with nitrogen products tank is arranged in the gas-liquid separator 10, makes in space division system starting With liquid nitrogen enters the space division system of cold energy of liquefied natural gas in extraction liquid nitrogen storage tank, facilitates and opens key equipment circulating liquid nitrogen pump 9。
The main heat exchanger 4, liquefaction heat exchanger 5, LNG- nitrogen heat exchanger 11 are plate heat exchangers, and are by individual one It is a or be made of multiple points of heat exchangers, avoid Temperature cross-over in heat exchanger.
Embodiment two:
A kind of space division system progress air separating method using cold energy of liquefied natural gas, comprising the following steps:
A) raw air compresses after self-cleaning strainer 1 removes most of solid impurity into air compressor 2, by dividing Sub- screen system 3 obtains pure air 103 after removing the impurity such as water removal, hydrocarbon；
B) pure air 103 is in main heat exchanger 4 by extracting out with upper 8 top of tower and providing cooling capacity simultaneously in liquefaction heat exchanger 5 The dirty nitrogen 402 and cycle of higher pressure liquid nitrogen 501 of preliminary re-heat exchange heat and are cooled and liquefy.The complete re-heat in main heat exchanger Dirty nitrogen 403 connects purification system 3 and does regeneration gas and cold blowing gas；
C) air 104 after liquefying provides cooling capacity in liquefaction heat exchanger 5 for liquefaction pressure nitrogen 205 and 208, and re-heat is Gas-liquid mixed air 105, which enters in rectifying tower system, is separated into discharge logistics, and the discharge logistics includes obtaining at the top of upper tower 7 Pure nitrogen gas 202 and liquid nitrogen product 218, the dirty nitrogen 401 that is obtained from upper 7 top of tower, the liquid oxygen 301 obtained from upper tower bottom；
D) raw air 105 obtains oxygen-enriched liquid air 106 in lower 6 bottom of tower in lower tower 6 after initial gross separation, at lower 6 top of tower Medium pressure nitrogen gas is obtained, medium pressure nitrogen gas enters main condenser evaporator 7, liquid nitrogen is condensed by the liquid oxygen of upper 8 bottom of tower, the one of the liquid nitrogen Part sends lower tower 6 back to maintain the rectifying operating condition of lower tower 6, and the throttling of another part liquid nitrogen 201 is sent at the top of upper tower 8 and participates in rectifying； In addition it extracts one pressure nitrogen gas 208 out and enters liquefaction heat exchanger 5, lower tower 6 is returned after being liquefied and does phegma；Oxygen-enriched liquid air 106 It is sent into after throttling in the middle part of upper tower 8 and participates in the rectifying of upper tower 8；
E) it is sent into the gas oxygen progress rectifying again that liquid nitrogen 201, oxygen-enriched liquid air 106 and the main condenser evaporator 7 of upper tower evaporate, from Obtain low-pressure nitrogen 202 and liquid nitrogen 218 at the top of upper tower 8, obtain dirty nitrogen 401 from upper 8 top of tower, main condenser evaporator 7 it is upper Portion is connected to upper 8 bottom of tower, obtains liquid oxygen in upper 8 bottom of tower, and extraction is the liquid oxygen 301 of gasification from main condenser evaporator 7, is sent It is used as product liquid oxygen out；The dirty nitrogen 401 obtained from upper 8 top of tower re-heat in liquefaction heat exchanger 5 and main heat exchanger 4 heats up out It is divided into two-way after air gas separation unit, dirty nitrogen goes type air purifier 3 to make regeneration gas through regenerating hot-air heater 16 all the way, all the way Vent muffler is gone to be vented as dirty nitrogen is vented；If space division has ar system, Argon fraction is obtained in the middle part of upper tower, Argon fraction is sent Enter full distillation non hydrogen argon producing system and produce product liquid argon, which is known to industry technical staff, herein no longer It is tired to state；
F) a part of liquid nitrogen 213 obtained in gas-liquid separator 10 is pressurised into supercritical pressure liquid nitrogen into circulating liquid nitrogen pump 9 501 and enter 4 re-heat of main heat exchanger be room temperature after, overcritical liquid nitrogen is cooled to by high pressure LNG602 into LNG- nitrogen heat exchanger 11 503, obtain LNG cold energy；Enter 13 expanding end of liquid booster expansion machine after liquefaction and is expanded to low-pressure gas-liquid mixing nitrogen 210, into Enter gas-liquid separator 10 and is separated into nitrogen 211 and liquid nitrogen；The pure nitrogen gas 202 extracted out at the top of upper tower 8 is changed with nitrogen 211 into liquefaction Hot device 5 provides cooling capacity, and nitrogen 203 is mixed into after re-heat and enters 13 pressurized end boil down to low-pressure nitrogen of liquid booster expansion machine 204, the further cooling of liquefaction heat exchanger 5 is entered back into after being cooled into LNG- nitrogen heat exchanger 11 and is liquefied as liquid nitrogen 206, throttling Enter gas-liquid separator 10 afterwards, is mixed into liquid nitrogen 212 with the liquid nitrogen separated after expansion；
G) tri- tunnel 212 Fen Wei of liquid nitrogen in gas-liquid separator 10, circulating liquid nitrogen 213, nitrogen products 217 and the cold liquid nitrogen 214 of benefit；It follows 213 flow of ring liquid nitrogen immobilizes, and when LNG601 meets requirement of system design, mending cold 214 flow of liquid nitrogen is 0, works as LNG601 When flow is higher than design temperature or two kinds of situations while occurring lower than design discharge or temperature, product liquid is reduced by actual conditions 217 flow of nitrogen increases and mends cold 214 flow of liquid nitrogen, to maintain system stable operation；It, can also be by starting liquid nitrogen under extreme case 216 pipeline is mended cold using liquid nitrogen in storage tank；
H) LNG601 gasifies after exchanging heat to go out the natural gas 604 and 605 of LNG- nitrogen heat exchanger 11, middle 604 temperature of pumping natural gas It is still below 0 degree, is exchanged heat in ethylene glycol heat exchanger 12 after mixing LNG603 with glycol water 701, LNG603 and day are obtained Cooling medium of the glycol water 703 of 604 cold energy of right gas as air compressor machine 2 interstage cooler and aftercooler, heat exchange Glycol water 702 afterwards pressurizes through ethylene glycol solution circulating pump 15, returns ethylene glycol heat exchanger 12 and carries out cycle heat exchange, LNG603 and natural gas 604 are warming up to normal-temperature natural-gas 606 and mix feeding gas distributing system 607 with natural gas 605.
Although the embodiment of the present invention is described with above attached drawing, the invention is not limited to above-mentioned Specific embodiment, the above mentioned embodiment is only schematical, is not restrictive, the ordinary skill of this field Personnel under the inspiration of the present invention, without breaking away from the scope protected by the purposes and claims of the present invention, can also do Many forms out, within these are all belonged to the scope of protection of the present invention.

Claims (10)

1. a kind of space division system using cold energy of liquefied natural gas, it is characterised in that: including air gas separation unit, LNG cold energy benefit With unit and ethylene glycol solution circulating cooling unit；
The ethylene glycol solution circulating cooling unit includes LNG- ethylene glycol heat exchanger (12) and ethylene glycol solution circulating pump (15)；
The LNG cold energy use unit includes that circulating liquid nitrogen pumps (9), LNG- nitrogen heat exchanger (11), gas-liquid separator (10), liquid Booster expansion machine (13) and vent muffler (17)；
The air gas separation unit adds comprising self-cleaning air filter (1), air compressor (2), molecular sieve (3), regeneration gas Hot device (14), main heat exchanger (4), liquefaction heat exchanger (5), rectifying column and vent muffler (16), rectifying column include lower tower (6), Main condenser evaporator (7) and upper tower (8) three parts.
2. a kind of space division system using cold energy of liquefied natural gas according to claim 1, which is characterized in that the air In separative unit:
Self-cleaning air filter (1) outlet is connected with air compressor (2) entrance；Molecular sieve (3) entrance and pneumatics Machine (2) outlet is connected with vent muffler (16)；Molecular sieve (3) outlet and main heat exchanger (4) and regeneration hot-air heater (14) phase Even；
Main heat exchanger (4) hot end and cold end have three strands, hot end respectively with molecular sieve (3) outlet, LNG- nitrogen heat exchanger (11) hot end is connected with regeneration hot-air heater (14)；Cold end respectively with a hot end of liquefaction heat exchanger (5) and a cold end, follow The outlet of ring liquid nitrogen pump (9) is connected；
Liquefaction heat exchanger (5) hot end and cold end have six strands；Cold end respectively with main heat exchanger (4) cold ends, a upper towers (8) top is connected with top, lower tower (6) top, gas-liquid separator (10) top with top；Hot end respectively with lower tower (6) bottom With top, a cold end of main heat exchanger (4), a hot end of LNG- nitrogen heat exchanger (11) and liquid booster expansion machine (13) End entrance is pressurized to be connected；
The top of the lower tower (6) be equipped with two groups of outlets and entrance, wherein one group respectively with the hot end of main condenser evaporator (7) and Cold end is connected, and another group is connected with the hot end of liquefaction heat exchanger (5) and cold end respectively；Bottom inlet and liquefaction heat exchanger (5) heat End is connected, and outlet at bottom is connected through throttle valve with upper tower (8) top；
It is connected at the top of main condenser evaporator (7) entrance and lower tower (6), outlet is divided into three strands, pushes up respectively with lower tower (6) Portion, product liquid oxygen storage tank and through being connected at the top of throttle valve and upper tower (8)；
Upper tower (8) outlet is divided into three strands, is that top first outlet is connected with nitrogen products storage tank respectively, top second goes out Mouth and upper outlet are connected with two bursts of cold ends of liquefaction heat exchanger (5) respectively；Top and top two entrances respectively with main condenser Evaporator (7) (6) bottom He Xiata is connected.
3. a kind of space division system using cold energy of liquefied natural gas according to claim 2, it is characterised in that: the molecule Sieve (3) is divided into two, is used alternatingly, one regeneration of a purifying；The entrance for purifying end is connected with air compressor machine (2) outlet, purifies The outlet at end is connected with the hot end of main heat exchanger (4)；The entrance caused trouble again is connected with regeneration hot-air heater (14) outlet, then causes trouble Outlet be connected with vent muffler (16).
4. a kind of space division system using cold energy of liquefied natural gas according to claim 1, which is characterized in that the second two In alcoholic solution circulating cooling unit:
The LNG- ethylene glycol heat exchanger (12) hot end and cold end have two strands, two stocks of cold end not with cryogenic natural gas pipeline Be connected with air compressor machine (2) interstage cooler with aftercooler entrance, two stocks in hot end not with natural gas line and ethylene glycol Solution circulation pump (15) outlet is connected；
Ethylene glycol solution circulating pump (15) entrance is connected with air compressor machine (2) interstage cooler and aftercooler outlet, out Mouth is connected with LNG- ethylene glycol heat exchanger (12) hot end.
5. a kind of space division system using cold energy of liquefied natural gas according to claim 1, which is characterized in that the LNG In cold energy use unit:
Circulating liquid nitrogen pump (9) entrance is connected with gas-liquid separator (10) bottom, and outlet is connected with main heat exchanger (4) cold end；
Gas-liquid separator (10) top exit is connected with (5) two bursts of cold ends of liquefaction heat exchanger respectively with one, top entrance, Another entrance of top is connected with liquid nitrogen product storage tank, and outlet at bottom pumps (9) entrance, nitrogen products storage tank with circulating liquid nitrogen respectively It is connected with LNG- nitrogen heat exchanger (11)；Centre entrance is connected with the outlet of liquid booster expansion machine (13) expanding end；
The liquid booster expansion machine (13) is divided into pressurized end and expanding end, the pressurization end entrance and liquefaction heat exchanger (5) two A hot end is connected, and outlet is connected with LNG- nitrogen heat exchanger (11) hot end；The expansion end entrance and LNG- nitrogen heat exchanger (11) are cold End is connected, and outlet is connected with gas-liquid separator (10)；
LNG- nitrogen heat exchanger (11) cold end have five strands, hot end have four strands, cold end respectively with LNG pipeline, liquefaction heat exchanger (5) Hot end, liquid booster expansion machine (13) expansion end entrance, LNG- ethylene glycol heat exchanger (12) and gas-liquid separator (10) bottom phase Even；Hot end disappears with natural gas line, the outlet of liquid booster expansion machine (13) pressurized end, main heat exchanger (4) hot end and emptying respectively Sound device (17) is connected.
6. a kind of space division system using cold energy of liquefied natural gas according to claim 5, it is characterised in that: the LNG- One heat exchanger channels is arranged in nitrogen heat exchanger (11), and both ends are connected with gas-liquid separator (10) and vent muffler (17) respectively, It opens and uses when LNG cold energy deficiency；Heat exchange gas channel middle extracts one natural gas (604) out, inputs LNG- second to adjust The cooling capacity of glycol heat exchanger (12).
7. a kind of space division system using cold energy of liquefied natural gas according to claim 5, it is characterised in that: the gas-liquid One pipeline (216) being connected with nitrogen products tank is arranged in separator (10), uses in space division system starting.
8. a kind of space division system using cold energy of liquefied natural gas according to claim 2 or 5, it is characterised in that: described Main heat exchanger (4), liquefaction heat exchanger (5), LNG- nitrogen heat exchanger (11) are by individual one or by multiple points of heat exchangers Composition, avoid Temperature cross-over in heat exchanger.
9. a kind of utilize a kind of space division system using cold energy of liquefied natural gas described in claim 1~8 any one claim The method that system carries out air separation, it is characterised in that: the following steps are included:
A) raw air compresses after self-cleaning strainer (1) removes most of solid impurity into air compressor (2), leads to Over-molecular sieve system (3) obtains pure air (103) after removing the impurity such as water removal, hydrocarbon；
B) pure air (103) is in main heat exchanger (4) by extracting out with upper tower (8) top and mentioning in liquefaction heat exchanger (5) The dirty nitrogen (402) and cycle of higher pressure liquid nitrogen (501) of semen donors and preliminary re-heat exchange heat and are cooled and liquefy；In main heat exchanger In completely re-heat dirty nitrogen (403) connection purification system (3) do regeneration gas and cold blowing gas；
C) air (104) after liquefying provides cooling capacity in liquefaction heat exchanger (5) for liquefaction pressure nitrogen (205) and (208), and Re-heat enters in rectifying tower system for gas-liquid mixed air (105) is separated into discharge logistics, and the discharge logistics includes from Shang Ta (7) pure nitrogen gas (202) and liquid nitrogen product (218) that are obtained at the top of, the dirty nitrogen (401) obtained from Shang Ta (7) top, from Shang Ta The liquid oxygen (301) that bottom obtains；
D) raw air (105) obtains oxygen-enriched liquid air (106) in Xia Ta (6) bottom, under in Xia Ta (6) after initial gross separation Medium pressure nitrogen gas is obtained at the top of tower (6), medium pressure nitrogen gas enters main condenser evaporator (7), is condensed into liquid by the liquid oxygen of upper tower (8) bottom Nitrogen, a part of the liquid nitrogen send Xia Ta (6) back to maintain the rectifying operating condition of lower tower (6), and another part liquid nitrogen (201) throttling is sent into Rectifying is participated at the top of upper tower (8)；In addition one pressure nitrogen gas (208) is extracted out into liquefaction heat exchanger (5), under returning after being liquefied Tower (6) does phegma；It is sent into after oxygen-enriched liquid air (106) throttling in the middle part of upper tower (8) and participates in the rectifying of upper tower (8)；
E) liquid nitrogen (201), oxygen-enriched liquid air (106) and the gas oxygen of main condenser evaporator (7) evaporation for being sent into upper tower carry out again Secondary rectifying obtains low-pressure nitrogen (202) and liquid nitrogen (218) from the top Shang Ta (8), obtains dirty nitrogen from Shang Ta (8) top (401), the top of main condenser evaporator (7) is connected to upper tower (8) bottom, obtains liquid oxygen in Shang Ta (8) bottom, is steamed from main condenser The liquid oxygen (301) that extraction is unvaporized in device (7) is sent out, sends out and is used as product liquid oxygen；The dirty nitrogen obtained from Shang Ta (8) top (401) re-heat heats up out and is divided into two-way after air gas separation unit in liquefaction heat exchanger (5) and main heat exchanger (4), all the way dirty nitrogen Gas goes type air purifier (3) to make regeneration gas through regenerating hot-air heater (16), goes vent muffler to put as the dirty nitrogen of emptying all the way It is empty；If space division has ar system, Argon fraction is obtained in the middle part of upper tower, Argon fraction is sent into argon producing system and produces product liquid argon；
F) a part of liquid nitrogen (213) obtained in gas-liquid separator (10) is pressurised into overcritical pressure into circulating liquid nitrogen pump (9) Power liquid nitrogen (501) and enter main heat exchanger (4) re-heat be room temperature after, it is cold by high pressure LNG (602) into LNG- nitrogen heat exchanger (11) It but is overcritical liquid nitrogen (503) to obtain LNG cold energy；Enter liquid booster expansion machine (13) expanding end after liquefaction and is expanded to low pressure Gas-liquid mixed nitrogen (210) is separated into nitrogen (211) and liquid nitrogen into gas-liquid separator (10)；That extracts out at the top of upper tower (8) is pure Nitrogen (202) and nitrogen (211) enter liquefaction heat exchanger (5) and provide cooling capacity, and nitrogen (203) is mixed into after re-heat and enters liquid Booster expansion machine (13) pressurized end boil down to low-pressure nitrogen (204) enters back into liquid after being cooled into LNG- nitrogen heat exchanger (11) Change heat exchanger (5) it is further cooling and liquefy as liquid nitrogen (206), enter gas-liquid separator (10) after throttling, and separated after expansion Liquid nitrogen be mixed into liquid nitrogen (212)；
G) liquid nitrogen (212) is divided into three tunnels, circulating liquid nitrogen (213), nitrogen products (217) and the cold liquid of benefit in gas-liquid separator (10) Nitrogen (214)；Circulating liquid nitrogen (213) flow immobilizes, and when LNG (601) meets requirement of system design, mends cold liquid nitrogen (214) Flow is 0, when LNG (601) flow is higher than design temperature or two kinds of situations while occurring lower than design discharge or temperature, is pressed Actual conditions reduce nitrogen products (217) flow, increase and mend cold liquid nitrogen (214) flow, to maintain system stable operation；Extreme feelings Under condition, the liquid nitrogen in storage tank also can be used to mend cold；
H) LNG (601) gasifies after exchanging heat to go out the natural gas (604) of LNG- nitrogen heat exchanger (11) and (605), middle part extraction Natural gas (604) temperature is still below 0 degree, mixes LNG (603) afterwards with glycol water (701) in ethylene glycol heat exchanger (12) Middle heat exchange, the glycol water (703) for obtaining LNG (603) and natural gas (604) cold energy are used as air compressor machine (2) cascade EDFA The cooling medium of device and aftercooler, the glycol water (702) after heat exchange pressurize through ethylene glycol solution circulating pump (15), It goes back to ethylene glycol heat exchanger (12) and carries out cycle heat exchange, LNG (603) and natural gas (604) are warming up to normal-temperature natural-gas (606) and day Gas distributing system (607) are sent into right gas (605) mixing.
10. the method that a kind of space division system using cold energy of liquefied natural gas according to claim 9 carries out air separation, It is characterized by: supercritical steam cycle nitrogen (502) pressure is higher than LNG (601)；It is arranged on the nitrogen (205) pipeline There is chain hydrocarbon detector of alarming.
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