CN100494839C - Air separation system for generating liquid oxygen and liquid nitrogen - Google Patents

Air separation system for generating liquid oxygen and liquid nitrogen Download PDF

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Publication number
CN100494839C
CN100494839C CNB2007100679826A CN200710067982A CN100494839C CN 100494839 C CN100494839 C CN 100494839C CN B2007100679826 A CNB2007100679826 A CN B2007100679826A CN 200710067982 A CN200710067982 A CN 200710067982A CN 100494839 C CN100494839 C CN 100494839C
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China
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nitrogen
liquid
heat exchanger
air
natural gas
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CNB2007100679826A
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Chinese (zh)
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CN101033909A (en
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卢杰
毛绍融
朱朔元
何晖
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杭州杭氧股份有限公司
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
    • F25J1/0292—Refrigerant compression by cold or cryogenic suction of the refrigerant gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F25J1/0015—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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F25J1/0224—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0228—Coupling of the liquefaction unit to other units or processes, so-called integrated processes
    • F25J1/0234—Integration with a cryogenic air separation unit
    • 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
    • F25J3/04151—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
    • F25J3/04151—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
    • F25J3/0423—Subcooling of liquid process 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
    • 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
    • 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
    • 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
    • F25J2230/08—Cold compressor, i.e. suction of the gas at cryogenic temperature and generally without afterstage-cooler
    • 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
    • F25J2230/60—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being hydrocarbons or a mixture of hydrocarbons
    • 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
    • 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
    • F25J2250/50—One fluid being oxygen

Abstract

This kind of air separation system obtaining liquid oxygen and liquid nitrogen at least includes an air separator mainly consisting of a fractionating tower and at least includes an equipment for recovering cold energy of liquefied natural gas mainly consisting of an liquefied natural gas heat exchanger, which still includes main heat exchanger, liquid-oxygen heat exchanger and liquid-nitrogen liquid air subcooler; oxygen is drawn out from the underpart of the upper column on the fractionating tower, and cools and liquefied in the liquid-oxygen heat exchanger as the liquid oxygen products; after nitrogen from the top of the upper column passes through a liquid-nitrogen liquid air subcooler and is reheated by main heat exchanger, some nitrogen enters into liquefied-natural-gas heat exchanger to recool and exchange heat to become high pressure nitrogen through primary compression and pressurization at least. And through throttling expansion and air-liquid separator, nitrogen and liquid nitrogen participate in recycling and other nitrogen as liquid-nitrogen products; energy consumption is reduced notably after using actually, power consumption which produces liquid oxygen of 1kg is 0.39kwh, while the power consumption of the traditional equal air separator is 1.0 to 1.25kwh, which is 2.4 to 3 times than the separator. And it is easy to popularize and apply.

Description

Obtain the air-seperation system of liquid oxygen and liquid nitrogen

Technical field

The present invention relates to a kind of cold energy of liquefied natural gas that reclaims to obtain the air-seperation system of liquid oxygen and liquid nitrogen, be applicable to a large amount of productions of liquid oxygen, liquid nitrogen and argon cut, can reduce the energy consumption of air separation process significantly.

Background technology

The main component of air is nitrogen and oxygen, is the inexhaustible source of industrial preparation nitrogen and oxygen.Oxygen is mainly used in the oxidant in metallurgy, combustion-supporting gas, medical treatment, wastewater treatment and the chemical industry etc.Nitrogen is mainly used in protective atmosphere, the protection of the inertia in Chemical Manufacture gas (nitrogen of blow line, readily oxidizable substance envelope, binder during the start-stop car), grain stocking, fruit freshness preserving and the electronics industry etc. of synthetic ammonia, metal heat treatmet.The conventional method of industrial separation of air is to adopt separation by deep refrigeration, is about to air and is cooled to its liquefaction point under certain pressure, and the method with low-temperature fractionation realizes separating again.This method can obtain oxygen and nitrogen, perhaps liquid oxygen, liquid nitrogen simultaneously.But, air separation process carries out under cryogenic conditions usually, and (80～100K) all is to be obtained by power-actuated mechanical refrigeration to low temperature environment, produces these colds and need consume a large amount of electric power, especially when producing a large amount of liquid oxygen, liquid nitrogen, energy consumption will significantly increase.Therefore, how at an easy rate separation of air is produced oxygen and nitrogen, and this is to be badly in need of the problem researched and solved in recent ten years.

Liquefied natural gas (Liquefied Natural Gas LNG) is the depickling of natural gas (principal component is methane, ethane etc.) process, processed, and the liquid mixture that low-temperature liquefaction obtains, its minimum temperature is-162 ℃.Liquefied natural gas could use after generally will vaporizing by vaporizer, and discharges a large amount of colds in vaporescence.And these colds all are to obtain by the mechanical energy consumption in the liquefaction process, if cold recovery and alternative mechanical refrigeration with liquefied natural gas, can reduce the power consumption in liquid oxygen, the liquid nitrogen production process, not only can avoid the waste of the energy, can also obtain great economic benefit.Under 8MPa pressure, liquefied natural gas is 830kJ/kg from-162 ℃ of colds that discharge when vaporizing 27 ℃ of environment temperatures.The electric consumption that traditional air-separating plant is produced the 1kg liquid oxygen is 1.0～1.2kwh, and the cold energy of liquefied natural gas recovery is used for air-separating plant, and the electric consumption of every 1kg liquid oxygen can reduce to below the 0.5kwh, has significantly reduced production cost.Therefore, reclaiming cold energy of liquefied natural gas is an energy-saving and cost-reducing important development direction of air separation field.

China utility model patent CN2,499,774Y has described a kind of air-separating plant.This air-separating plant comprises multistage circulating nitrogen gas compressor, liquefied natural gas heat exchanger, circulating nitrogen gas heat exchanger, and the cooling cycle system of interior circulation of composition nitrogen and nitrogen outer circulation, utilize the circulating nitrogen gas of liquefied natural gas cooling low temperature compression and normal temperature compressed air.Similar with it, U.S. Pat 5,137,558A has described a kind of air-separating plant.This air-separating plant utilizes liquefied natural gas precooling raw air and cycle of higher pressure nitrogen, separates after the high pressure nitrogen throttling to obtain liquid nitrogen, and it is interior as withdrawing fluid that liquid nitrogen enters fractionating column, and the cold of air separation is provided.U.S. Pat 5,220,798A has described a kind of air-separating plant, and the part liquid nitrogen of producing in the past in can be by air-separating plant when cold that liquefied natural gas provides is not enough is replenished, circulating nitrogen gas after compression provides cold jointly, can guarantee the normal volume of liquid oxygen, liquid nitrogen.

Describe the air-separating plant that reclaims cold energy of liquefied natural gas above, reduced the energy consumption that obtains liquid oxygen and liquid nitrogen significantly.Should be pointed out that air-separating plant inside is an oxygen concentration district, liquefied natural gas is rich in hydrocarbons such as methane, belongs to inflammable easily fried material, and the air-separating plant that reclaims cold energy of liquefied natural gas is very high to security requirement.Liquefied natural gas is belonging to combustible, should avoid in the removal process liquefied natural gas directly with air-separating plant in air, oxygen, liquid oxygen carry out heat exchange, these materials may with the liquefied natural gas formation damp that leaks.Therefore, reclaim the security of the process palpus assurance air-separating plant of cold energy of liquefied natural gas.

Summary of the invention

The objective of the invention is to overcome the deficiency of above-mentioned existence, and provide a kind of utilize reclaim cold energy of liquefied natural gas, with conserve energy, the acquisition liquid oxygen that efficient is provided and the air-seperation system of liquid nitrogen.

The objective of the invention is to finish by following technical solution, which comprises at least an air-separating plant of mainly forming by fractionating column and comprise a main cold energy of liquefied natural gas retracting device of forming by the liquefied natural gas heat exchanger at least, also dispose main heat exchanger, liquid oxygen heat exchanger and liquid nitrogen liquid air subcooler in the described air-separating plant; Draw oxygen tower bottom from the fractionation of fractionating column, and cooling liquid in the liquid oxygen heat exchanger, as the liquid oxygen product; After the re-heat of the nitrogen that top of tower is drawn from the fractionation of fractionating column through liquid nitrogen liquid air subcooler, main heat exchanger, entering the liquefied natural gas heat exchanger after having at least part through the compression of one-level at least supercharging carries out precool heat exchanger and becomes high pressure nitrogen, after throttling expansion, again through gas-liquid separator, nitrogen and part liquid nitrogen participate in nitrogen circulation, and all the other liquid nitrogen are as liquid nitrogen product.

Also include vapour liquid separator and liquid nitrogen subcooler in the described cold energy of liquefied natural gas retracting device, and dispose low-pressure nitrogen compressor, middle pressure nitrogen compressor and three grades of compressions of high pressure nitrogen compressor supercharging at least, and liquefied natural gas heat exchanger, vapour liquid separator and liquid nitrogen subcooler are placed in one independently in the ice chest II; And main heat exchanger, liquid oxygen heat exchanger, liquid nitrogen liquid air subcooler and by tower under the fractionation, the fractionating column that tower and main condenser evaporimeter connect to form in the fractionation is placed in one independently in the ice chest I.

Described nitrogen of being drawn by top of tower in the fractionation, after the re-heat of liquid nitrogen liquid air subcooler, (M1-M2) re-heat, part also is introduced into ice chest II, sends into the compression of low pressure nitrogen turbocompressor in the lump with other nitrogen to enter the nitrogen heat exchanger channels of main heat exchanger.

Describedly draw dirty nitrogen by tower top in the fractionation, after the re-heat of liquid nitrogen liquid air subcooler, (B1-B2) continue re-heat draws ice chest I afterwards to enter the dirty nitrogen heat exchanger channels of main heat exchanger; The dirty nitrogen of cooling box I can be by after electric heater or the Steam Heating, delivers in the molecular sieve purifier as regeneration gas, and the water of desorption molecular sieve adsorption, carbon dioxide discharge atmospheric environment then.

Described middle and lower part by tower in the fractionation is drawn and is contained the higher argon cut of argon amount, removes to make the argon device as the raw material that obtains liquid argon or other form argon product.

The described nitrogen that top of tower is drawn from the fractionation is through the liquid nitrogen liquid air subcooler, after the main heat exchanger re-heat, with merge from vapour liquid separator and through the nitrogen of re-heat, raw nitrogen gas as liquefaction of nitrogen, enter subsequently in the low pressure nitrogen turbocompressor and be compressed to 0.4～0.6MPa, with converge from vapour liquid separator and the circulating nitrogen gas after the re-heat of liquefied natural gas heat exchanger, press in entering in the nitrogen turbocompressor and be compressed to 2.0～4.0MPa, enter the precooling of liquefied natural gas heat exchanger subsequently; The nitrogen that leaves the liquefied natural gas heat exchanger enters and is compressed to 5.0～7.0MPa and throttling expansion in the elevated pressure nitrogen turbocompressor, produces the damp steam that contains liquid nitrogen, removes vapour liquid separator, finishes the nitrogen kind of refrigeration cycle; Liquefied natural gas is drawn ice chest II after by re-heat and is used for other purposes in the liquefied natural gas heat exchanger;

Describedly return the re-heat of liquefaction heat exchange gas device, merge with raw nitrogen gas and press the nitrogen turbocompressor in going by the vapour liquid separator separated nitrogen.By the isolated liquid nitrogen of vapour liquid separator through liquid nitrogen subcooler cross cold after, liquid nitrogen subcooler, the re-heat of liquefied natural gas heat exchanger are returned in a part of throttling expansion successively, the nitrogen of drawing with ice chest I converges the low pressure nitrogen turbocompressor; A part is drawn ice chest II, is sent to liquid nitrogen storage as liquid nitrogen product; Return ice chest I after all the other nitrogen throttling expansions, the low pressure nitrogen turbocompressor is removed in re-heat in liquid oxygen heat exchanger, main heat exchanger successively, finishes nitrogen circulation.

Pressing nitrogen turbocompressor (16) and elevated pressure nitrogen turbocompressor (17) in described is the low temperature turbocompressor, and is positioned at the outside of ice chest II (2); The middle nitrogen turbocompressor of pressing, the elevated pressure nitrogen turbocompressor, the heat exchanger channels of liquefied natural gas heat exchanger, choke valve constitutes the nitrogen refrigeration cycle.

The refrigerant that the nitrogen that air separation is come out transmits as cold and no longer enters tower in the fractionation after the liquefied natural gas heat exchange, perhaps tower under the fractionation guarantees the safe operation of air-separating plant.

The pressure of described liquefied natural gas can enter the heat exchanger channels (H1-H2), draw ice chest II after the re-heat of liquefied natural gas heat exchanger in 4.0～9.5MPa scope.

The present invention has made full use of the high-grade cold energy of liquefied natural gas, obtain liquid oxygen and liquid nitrogen, the energy consumption of air-separating plant significantly reduces, the electric consumption of producing the 1kg liquid oxygen is 0.39kwh, and the traditional air-separating plant of equal scale to produce the electric consumption of 1kg liquid oxygen be 1.0～1.25kwh, be 2.4～3 times of air-separating plant unit power consumption amount proposed by the invention; Therefore patent of the present invention if can be applied, and will obtain great economic benefit work.

Description of drawings

Accompanying drawing 1 is a whole system syndeton schematic diagram of the present invention.

The specific embodiment

Serial number name is among Fig. 1: 1-ice chest I, 2-ice chest II, 3-main heat exchanger, tower under 4-fractionation, 5-main condenser evaporimeter, tower in 6-fractionation, 7-liquid air liquid nitrogen subcooler, 8-liquid nitrogen choke valve, 9-liquid air choke valve, 10-liquid oxygen heat exchanger, 11-liquid nitrogen subcooler, 12-gas-liquid separator, 13-choke valve, 14-liquefied natural gas heat exchanger, 15-low pressure nitrogen turbocompressor, 16-middle pressure nitrogen turbocompressor, 17-elevated pressure nitrogen turbocompressor, 18-liquid oxygen storage tank, 19-liquid nitrogen storage

Relevant logistics numbering: 101-elevated pressure nitrogen turbocompressor compression, introduce the circulating nitrogen gas of liquefied natural gas heat exchanger heat exchange, 102-middle pressure nitrogen turbocompressor compression, introduce the circulating nitrogen gas of liquefied natural gas heat exchanger heat exchange, 103-go out the circulating nitrogen gas of gas-liquid separator, 104-go out the liquid nitrogen product of liquid nitrogen subcooler, 105-go out the liquid nitrogen that liquid nitrogen subcooler is introduced ice chest I, 106-go out gas-liquid separator, introduce the liquid nitrogen of liquid nitrogen subcooler re-heat, 107-go out the circulating nitrogen gas of liquid nitrogen subcooler, 108-go out tower in the fractionation, raw nitrogen gas after the main heat exchanger re-heat, 109-go out tower in the fractionation, the dirty nitrogen after the main heat exchanger re-heat, 110-go out the liquid oxygen heat exchanger, circulating nitrogen gas after the main heat exchanger re-heat, 111-advance the liquefied natural gas of heat exchange gas device, 112-go out the liquefied natural gas of heat exchange gas device, 113-raw air of main heat exchanger entered, 114-tower is drawn from the fractionation argon cut, 115-tower is drawn from the fractionation oxygen cut.

The specific embodiment

The present invention will be described in detail below in conjunction with the accompanying drawings and the specific embodiments:

Main heat exchanger (3), fractionating column and liquid oxygen heat exchanger (10) are positioned at independently ice chest I (1) inside, reach fractionating column by tower under the fractionation (4), and tower in the fractionation (6) and main condenser evaporimeter (5) connect to form.

The raw air (113) of removing carbon dioxide, water, acetylene and other hydrocarbon impurity is admitted to the heat exchanger channels of the main heat exchanger (3) in the ice chest I (1) (A1-A2), the gas converting heat that backflows with other heat exchanger channels, after the temperature of suitable fractionation of cooling, send into the bottom of tower under the fractionation (4), at the multilayer column plate heat and mass transfer process takes place with withdrawing fluid under tower (4) overhead stream under fractionation.The higher oxygen enriched liquid air (abbreviation liquid air) of oxygen component comes together in the bottom of tower under the fractionation (4), and nitrogen comes together in the top of tower under the fractionation (4), and by the liquid oxygen institute condensation of the main condenser evaporimeter (5) between the tower (6) in tower under the fractionation (4) and the fractionation.

The liquid nitrogen that draw at tower (4) top under the fractionation is divided into two strands, one returns tower under the fractionation (4) as withdrawing fluid, another strand is cold excessively in liquid nitrogen liquid air subcooler (7), be depressurized to the pressure at tower in the fractionation (6) top through liquid nitrogen choke valve (8), and be admitted to tower in the fractionation (6) top, as the withdrawing fluid of tower in the fractionation (6).

Oxygen-enriched liquid air is drawn in tower (4) bottom under the fractionation, and is cold excessively in liquid nitrogen liquid air subcooler (7), is depressurized to the pressure at tower in the fractionation (6) middle part through liquid air choke valve (9), and is admitted to the middle part of tower in the fractionation (6), also as the withdrawing fluid of tower in the fractionation.

Above-mentioned two strands of withdrawing fluids become the withdrawing fluid of tower in the fractionation (6), at the multilayer column plate heat and mass transfer process take place with ascending air in tower, and the bottom of tower in fractionation (6) obtains liquid oxygen, and the top obtains nitrogen.Liquid oxygen is heated into oxygen by the nitrogen at tower under the fractionation (4) top in main condenser evaporimeter (5), oxygen becomes the main ascending air of tower in the fractionation (6), part oxygen is drawn tower in the fractionation (6) and is carried out next step liquefaction, perhaps draws ice chest I (1) as product.

Draw nitrogen by top of tower in the fractionation (6), after liquid nitrogen liquid air subcooler (7) re-heat, (M1-M2) re-heat, and be introduced into ice chest II (2) sends into low pressure nitrogen turbocompressor (16) compression in the lump with other nitrogen to enter the nitrogen heat exchanger channels of main heat exchanger (3).

Draw dirty nitrogen by tower in the fractionation (6) top, after liquid nitrogen liquid air subcooler (7) re-heat, (B1-B2) continues re-heat, draws ice chest I (1) afterwards to enter the dirty nitrogen heat exchanger channels of main heat exchanger (3).The dirty nitrogen of cooling box I (1) can be by after electric heater or the Steam Heating, delivers in the molecular sieve purifier as regeneration gas, and the water of desorption molecular sieve adsorption, carbon dioxide discharge atmospheric environment then.

Draw by the middle and lower part of tower in the fractionation (6) and to contain the higher argon cut (114) of argon amount, remove to make the argon device as the raw material that obtains liquid argon or other form argon product.

The nitrogen (110) that draw at tower (6) top from the fractionation is through liquid nitrogen liquid air subcooler (7), after main heat exchanger (3) re-heat, and merges from vapour liquid separator (12) and through nitrogen (107), the nitrogen (108) of re-heat, as the raw nitrogen gas of liquefaction of nitrogen; Enter compression in the low pressure nitrogen turbocompressor (15) subsequently, converge, press compression in the nitrogen turbocompressor (16) in entering with circulating nitrogen gas (103) from vapour liquid separator (12); Enter liquefied natural gas heat exchanger (14) subsequently by precooling, enter compression in the elevated pressure nitrogen turbocompressor (17) once more, and enter liquefied natural gas heat exchanger (14) and left liquefied natural gas heat exchanger (14) by precooling.

The high pressure nitrogen that leaves liquefied natural gas heat exchanger (14) produces the damp steam that contains liquid nitrogen by choke valve (13) throttling expansion, removes vapour liquid separator (12).

Return the re-heat of liquefaction heat exchange gas device (14) by vapour liquid separator (12) separated nitrogen (103), press the nitrogen turbocompressor in going with the nitrogen merging after low pressure nitrogen turbocompressor (15) compression.

By the isolated liquid nitrogen of vapour liquid separator (12) through liquid nitrogen subcooler (11) cross cold after, return liquid nitrogen subcooler (11), liquefied natural gas heat exchanger (14) re-heat successively after the part throttling expansion, the nitrogen of drawing with ice chest I (1) converges low pressure nitrogen turbocompressor (15), finishes nitrogen circulation; A part is drawn ice chest II (2), as liquid nitrogen product (104), and is sent to liquid nitrogen storage (18); Return ice chest I (1) after all the other liquid nitrogen (105) throttling expansion, in liquid oxygen heat exchanger (10), main heat exchanger (3), remove low pressure nitrogen turbocompressor (15) after the re-heat successively, finish nitrogen circulation.

Ice chest I (1) is drawn in the oxygen liquefaction that is cooled in liquid oxygen heat exchanger (10), as liquid oxygen product (103), and is sent to liquid oxygen storage tank (19).

Middle pressure nitrogen turbocompressor (16) is the low temperature turbocompressor with elevated pressure nitrogen turbocompressor (17), and is positioned at the outside of ice chest II (2).

The operating pressure of low pressure nitrogen turbocompressor (16) can be in 0.3～1.0MPa scope; The middle operating pressure of nitrogen turbocompressor (16) of pressing can be in 1.5～3.5MPa scope; The operating pressure of elevated pressure nitrogen turbocompressor (17) can be in 4.0～8.0MPa scope.

Liquefied natural gas heat exchanger (14), vapour liquid separator (12), liquid nitrogen subcooler (11) are positioned at independently ice chest II (2) inside.

Low pressure nitrogen turbocompressor (15), the middle nitrogen turbocompressor (16) of pressing, elevated pressure nitrogen turbocompressor (17), choke valve (13), the heat exchanger channels of liquefied natural gas heat exchanger (14) (D1-D2), (E1-E2), (F1-F2), (G1-G2), and the heat exchanger channels of main heat exchanger (3) (C1-C2), (M1-M2) constitutes the nitrogen refrigeration cycle.

The pressure of liquefied natural gas (111) can enter the heat exchanger channels (I1-I2), draw ice chest II (2) with gaseous form after the re-heat and be used for other purposes of liquefied natural gas heat exchanger (14) in 4.0～9.5MPa scope.

The foregoing description only is a preferred implementation of the present invention.For this air-separating plant that utilizes liquefied natural gas, can make various modification or optimization, these also are protection scope of the present invention.

Claims (10)

1, a kind of air-seperation system that obtains liquid oxygen and liquid nitrogen, which comprises at least an air-separating plant of mainly forming by fractionating column and comprise a main cold energy of liquefied natural gas retracting device of forming by the liquefied natural gas heat exchanger at least, it is characterized in that also disposing in the described air-separating plant main heat exchanger (3), liquid oxygen heat exchanger (10) and liquid nitrogen liquid air subcooler (7); Draw oxygen tower (6) bottom from the fractionation of fractionating column, and cooling liquid in liquid oxygen heat exchanger (10), as the liquid oxygen product; After the re-heat of the nitrogen that draw at tower (6) top from the fractionation of fractionating column through liquid nitrogen liquid air subcooler (7), main heat exchanger (3), entering the liquefied natural gas heat exchanger after having at least part through the compression of one-level at least supercharging carries out precool heat exchanger and becomes high pressure nitrogen, after throttling expansion, again through gas-liquid separator (12), nitrogen and part liquid nitrogen participate in nitrogen circulation, and all the other liquid nitrogen are as liquid nitrogen product.
2, the air-seperation system of acquisition liquid oxygen according to claim 1 and liquid nitrogen, it is characterized in that also including in the described cold energy of liquefied natural gas retracting device vapour liquid separator (12) and liquid nitrogen subcooler (11), and dispose low-pressure nitrogen compressor (15), middle pressure nitrogen compressor (16) and (17) three grades of compressions of high pressure nitrogen compressor supercharging at least, and liquefied natural gas heat exchanger, vapour liquid separator (12) and liquid nitrogen subcooler (11) are placed in one independently in the ice chest II (2); And main heat exchanger (3), liquid oxygen heat exchanger (10), liquid nitrogen liquid air subcooler (7) and by tower under the fractionation (4), the fractionating column that tower in the fractionation (6) and main condenser evaporimeter (5) connect to form is placed in one independently in the ice chest I (1).
3, the air-seperation system of acquisition liquid oxygen according to claim 1 and 2 and liquid nitrogen, it is characterized in that described nitrogen of drawing by tower in the fractionation (6) top, after liquid nitrogen liquid air subcooler (7) re-heat, enter the nitrogen heat exchanger channels (M1-M2) re-heat of main heat exchanger (3), part is introduced into ice chest II (2), sends into low pressure nitrogen turbocompressor (15) compression in the lump with other nitrogen.
4, the air-seperation system of acquisition liquid oxygen according to claim 3 and liquid nitrogen, it is characterized in that describedly drawing dirty nitrogen by tower in the fractionation (6) top, after liquid nitrogen liquid air subcooler (7) re-heat, (B1-B2) continues re-heat, draws ice chest I (1) afterwards to enter the dirty nitrogen heat exchanger channels of main heat exchanger (3); The dirty nitrogen of cooling box I (1) can be by after electric heater or the Steam Heating, delivers in the molecular sieve purifier as regeneration gas, and the water of desorption molecular sieve adsorption, carbon dioxide discharge atmospheric environment then.
5, the air-seperation system of acquisition liquid oxygen according to claim 3 and liquid nitrogen is characterized in that described middle and lower part by tower in the fractionation (6) is drawn and contains the higher argon cut of argon amount, removes to make the argon device as the raw material that obtains liquid argon or other form argon product.
6, the air-seperation system of acquisition liquid oxygen according to claim 4 and liquid nitrogen, it is characterized in that the described nitrogen that draw at tower (6) top from the fractionation is through liquid nitrogen liquid air subcooler (7), after main heat exchanger (3) re-heat, with merge from vapour liquid separator (12) and through the nitrogen of re-heat, raw nitrogen gas as liquefaction of nitrogen, enter subsequently in the low pressure nitrogen turbocompressor (15) and be compressed to 0.4～0.6MPa, with converge from vapour liquid separator (12) and the circulating nitrogen gas after the re-heat of liquefied natural gas heat exchanger, enter in the pressure nitrogen turbocompressor (16) and be compressed to 2.0～4.0MPa, enter the precooling of liquefied natural gas heat exchanger subsequently; The nitrogen that leaves the liquefied natural gas heat exchanger enters in the elevated pressure nitrogen turbocompressor (17) and is compressed to 5.0～7.0MPa and throttling expansion, produces the damp steam that contains liquid nitrogen, removes vapour liquid separator (12), finishes the nitrogen kind of refrigeration cycle; Liquefied natural gas is drawn ice chest II (2) after by re-heat and is used for other purposes in the liquefied natural gas heat exchanger.
7, the air-seperation system of acquisition liquid oxygen according to claim 6 and liquid nitrogen, it is characterized in that describedly returning the re-heat of liquefaction heat exchange gas device, merge with raw nitrogen gas and press nitrogen turbocompressor (16) in going by vapour liquid separator (12) separated nitrogen; By the isolated liquid nitrogen of vapour liquid separator (12) through liquid nitrogen subcooler (11) cross cold after, part throttling expansion, return liquid nitrogen subcooler (11), the re-heat of liquefied natural gas heat exchanger successively, the nitrogen of drawing with ice chest I (1) converges low pressure nitrogen turbocompressor (15); A part is drawn ice chest II (2), is sent to liquid nitrogen storage (18) as liquid nitrogen product; Return ice chest I (1) after all the other nitrogen throttling expansions, low pressure nitrogen turbocompressor (15) is removed in re-heat in liquid oxygen heat exchanger (10), main heat exchanger (3) successively, finishes nitrogen circulation.
8, the air-seperation system of acquisition liquid oxygen according to claim 7 and liquid nitrogen is characterized in that described middle pressure nitrogen turbocompressor (16) and elevated pressure nitrogen turbocompressor (17) are the low temperature turbocompressor, and is positioned at the outside of ice chest II (2); The middle heat exchanger channels of nitrogen turbocompressor (16), elevated pressure nitrogen turbocompressor (17), liquefied natural gas heat exchanger, the choke valve of pressing constitutes the nitrogen refrigeration cycle.
9, the air-seperation system of acquisition liquid oxygen according to claim 7 and liquid nitrogen, it is characterized in that the refrigerant that nitrogen that air separation comes out transmits as cold, with no longer enter tower (4) under tower in the fractionation (6) or the fractionation after the liquefied natural gas heat exchange, guarantee the safe operation of air-separating plant.
10, according to the air-seperation system of claim 7 or 8 described acquisition liquid oxygen and liquid nitrogen, it is characterized in that the liquefied natural gas pressure of flowing through in the described liquefied natural gas heat exchanger can be in 4.0～9.5MPa scope, enter the heat exchanger channels (H1-H2), draw ice chest II (2) after the re-heat of liquefied natural gas heat exchanger.
CNB2007100679826A 2007-04-11 2007-04-11 Air separation system for generating liquid oxygen and liquid nitrogen CN100494839C (en)

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Inventor after: Lu Jie

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Address after: No.799, Xiangfu Road, Qingshanhu street, Lin'an District, Hangzhou City, Zhejiang Province

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Patentee before: HANGZHOU HANGYANG Co.,Ltd.