CN109186179A - Full distillation proposes the oxygen-enriched air separation unit of argon and technique - Google Patents

Full distillation proposes the oxygen-enriched air separation unit of argon and technique Download PDF

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Publication number
CN109186179A
CN109186179A CN201811154245.4A CN201811154245A CN109186179A CN 109186179 A CN109186179 A CN 109186179A CN 201811154245 A CN201811154245 A CN 201811154245A CN 109186179 A CN109186179 A CN 109186179A
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argon
air
liquid
oxygen
nitrogen
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CN109186179B (en
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顾群超
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SUZHOU OXYGEN PLANT CO Ltd
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SUZHOU OXYGEN PLANT CO Ltd
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • 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
    • F25J3/0409—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 oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • 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
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    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04721—Producing pure argon, e.g. recovered from a crude argon column
    • F25J3/04727—Producing pure argon, e.g. recovered from a crude argon column using an auxiliary pure argon column for nitrogen rejection
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04963—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipment within or downstream of the fractionation unit(s)
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • 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
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/58—Processes or apparatus involving steps for recycling of process streams the recycled stream being argon or crude argon

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
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  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
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  • Separation By Low-Temperature Treatments (AREA)

Abstract

Full distillation provided by the invention mentions the oxygen-enriched air separation unit of argon, is related to air separation equipment field, including air pretreatment section, rectifying section and smart argon section；Rectifying section includes Xia Ta, upper tower, condenser/evaporator, main heat exchanger, supercharger/expanding machine, pressurization aftercooler, subcooler, the oxygen-enriched liquid air outlet of lower tower bottom is divided into two tunnels after connecting with the oxygen-enriched liquid air runner of subcooler, it connect with the oxygen-enriched liquid air import of upper tower, and is connect with crude argon condenser inlet；The liquid oxygen of upper tower bottom enters condenser/evaporator, and autocondensation evaporator outlet is divided into two tunnels, connects pure liquid oxygen product conveyance conduit as product liquid oxygen all the way, and another way and the oxygen-enriched liquid air outlet of liquid pump, lower tower bottom are sequentially connected；The argon fraction of upper tower lower part successively passes through the first crude argon column, the second crude argon column and pure argon column and obtains pure liquid argon；The beneficial effects of the invention are as follows oxygen-enriched air separation units to mention argon, increases device product kind, increases economic efficiency.

Description

Full distillation proposes the oxygen-enriched air separation unit of argon and technique
Technical field
The present invention relates to a kind of cryogenic air separation apparatus fields, and in particular to a kind of Full distillation mentions the oxygen-enriched air separation unit of argon And technique.
Background technique
Air refers to the gas mixing in earth atmosphere, it mainly by 78% nitrogen, 21% oxygen, 0.94% it is dilute Have gas (helium, neon, argon, krypton, xenon), 0.03% carbon dioxide, 0.03% other substances (such as vapor, impurity) composition Mixture, wherein rare gas is mainly argon ingredient.
Air separation plant is that air is raw material, and air is become liquid by the method for compression depth of round freezing, using Rectifying and from liquid air gradually separate produce the inert gases such as oxygen, nitrogen and argon gas equipment.Air separation plant is one The complication system of a large size mainly includes dynamical system, purification system, refrigeration system, heat-exchange system, distillation system, product Transportation system, liquid storage system and control system etc..
Dynamical system is primarily referred to as air compressor, and air is obtained the products such as oxygen, nitrogen through cryogenic separation by air separation plant, from It is essentially to be completed by energy conversion, and the energy of device is mainly inputted by air compressor；Purification system is by sky Gas chilldown system and sieve purification system composition, compressed raw air temperature is higher, and air precooling system is by connecing Touch heat exchange reduces the temperature of air, while can wash the objectionable impurities such as acidic materials therein, and sieve purification system is then It further removes moisture, carbon dioxide, acetylene, propylene, propane and nitrous oxide in air etc. and nocuousness is run to air separation plant Substance；The refrigeration system of air separation plant is realized by expanding machine, and the refrigeration of entire air separation plant follows strictly classical Refrigeration cycle；The thermal balance of air separation plant is completed jointly by refrigeration system and heat-exchange system, is exchanged heat in the prior art Device mainly uses aluminum plate-fin heat exchanger；The core of air separation plant is distillation system, realizes the cryogenic separation of composition of air, by Lower pressure column, medium pressure column and condenser/evaporator composition；The oxygen and nitrogen of air separation plant production need certain pressure to be just able to satisfy The use of follow-up system is completed by each road pipeline of product delivery system；The products such as the liquid oxygen and liquid nitrogen of air separation plant production, Into liquid storage system；Existing large air separation plant is all made of computer distributed control system, realizes and automatically controls.
The major product of this equipment is liquid nitrogen, liquid oxygen and oxygen-enriched air, and oxygen-enriched air is mainly used in converter, glass furnace Kiln, metal smelt etc. it is combustion-supporting.The general combustion-supporting pressure needed with oxygen-enriched air is in 0.1-0.2MPa.Conventional oxygen-enriched space division is set Standby to use twin-stage rectifying, upper tower bottom directly obtains oxygen rich gas and is forced into required pressure through oxygen compressor again after master changes re-heat, Or oxygen-enriched liquid air is obtained in upper tower bottom, to go out fractionating column cold for re-heat again after being pressurized to required pressure through compression in liquid oxygen pump or certainly Case.
The refrigeration system of existing air separation plant due to needing the dew point of each gas to be achieved, and then consumes a large amount of electricity Can, increase production cost；In addition, conventional oxygen-enriched air separation plant can produce byproduct purity nitrogen while obtaining oxygen rich air Air-liquid nitrogen can not produce purity oxygen or pure liquid oxygen simultaneously, and it is even more impossible to produce argon gas or liquid argon simultaneously.
Summary of the invention
It is an object of that present invention to provide a kind of Full distillations to mention the oxygen-enriched air separation unit of argon and technique, and Full distillation can be effectively reduced and mention The power consumption of the oxygen-enriched air separation process of argon, while the pure liquid nitrogen of byproduct and oxygen or liquid oxygen can also be produced simultaneously, and production liquid Argon or argon gas.
To reach above-mentioned purpose, the following technical solutions are proposed by the present invention: a kind of Full distillation mentions the oxygen-enriched air separation unit of argon, including Air pretreatment section, the air pretreatment section be used to prepare dry purified air and be transmitted to rectifying section；
It further include rectifying section and proposing argon section, the rectifying section includes Xia Ta, upper tower, condenser/evaporator, main heat exchanger, pressurization Aftercooler, supercharger, expanding machine and subcooler；The condenser/evaporator is arranged between Xia Ta and upper tower；It is described to propose argon section Including the first crude argon column, the second crude argon column, pure argon column, liquid pump, crude argon condenser, smart argon evaporator and smart argon condenser；
The dry purified air outlet of the air pretreatment section is divided into three tunnels, the first via and the first feeding air of main heat exchanger Runner, lower tower bottom air intlet are sequentially connected, the second tunnel and supercharger air inlet, pressurization aftercooler air inlet, main heat exchange Air intlet is sequentially connected in the middle part of the second feeding air of device runner, expander inlet and upper tower, third road and instrument air system Air inlet of uniting connects；
Two tunnels of the nitrogen outlet of the lower top of tower point, the first via are connect with condenser/evaporator air inlet；Second tunnel and essence The smart argon evaporator air inlet of argon column lower part connects；
The oxygen-enriched liquid air outlet of the lower tower bottom is divided into two tunnels, the first via after connecting with the oxygen-enriched liquid air runner of subcooler It is connect with the oxygen-enriched liquid air import on upper tower top, the second tunnel is connect with crude argon condenser inlet；
The condenser/evaporator liquid nitrogen runner exit is divided into two tunnels, and the first via is connect with the liquid nitrogen reflux mouth of lower top of tower, The connection of the liquid nitrogen runner of second tunnel and subcooler；
The liquid nitrogen runner exit of the subcooler is divided into three tunnels, and the first via is connect with upper top of tower liquid nitrogen reflux mouth, and second Road connects pure liquid nitrogen product conveyance conduit, third Lu Yujing argon condenser liquid nitrogen import connection as nitrogen products；
The upper tower bottom is connect with condenser/evaporator, and the liquid oxygen of upper tower bottom enters condenser/evaporator, liquid oxygen autocondensation Evaporator outlet is divided into two tunnels, and the first via connects pure liquid oxygen product conveyance conduit as product liquid oxygen, the second tunnel and liquid pump, under The oxygen-enriched liquid air outlet of tower bottom is sequentially connected, and the liquid after converging is connect with main heat exchanger liquid oxygen evaporation runner；
The dirty nitrogen on the upper tower top is connect with the dirty nitrogen runner of subcooler, main heat exchanger；
The purity nitrogen of the upper top of tower and the purity nitrogen of subcooler, main heat exchanger connect runner and connect；
The argon fraction outlet of the upper tower lower part and thick gas at the top of the first crude argon tower bottom argon fraction import, the first crude argon column Argon outlet and the thick gas argon import of the second crude argon tower bottom are sequentially connected；
Process argon outlet at the top of second crude argon column is divided into two tunnels, the first via and the import of crude argon condenser process argon and Second crude argon column crude argon refluxing opening is sequentially connected, and the second tunnel is connect with the process argon import in the middle part of pure argon column；
The pure liquid argon outlet of the pure argon column bottom connects pure liquid argon product conveyance conduit；
The essence argon condenser gas nitrogen and the outlet of upper tower top dirt nitrogen converge to be connected with the dirty nitrogen runner of subcooler, main heat exchanger It connects；
The crude liquid argon outlet of the second crude argon tower bottom is connect with liquid pump inlet, with crude liquid argon at the top of the first crude argon column Import connection flows back with the argon fraction of upper tower lower part and connects.
Further, the rectifying section includes liquid nitrogen producing line；The liquid nitrogen producing line goes out from air pretreatment section dry air Mouth is through the first feeding air of main heat exchanger runner, lower tower bottom air intlet, lower top of tower nitrogen outlet, condenser/evaporator nitrogen Import to condenser/evaporator liquid nitrogen exports；
The liquid nitrogen outlet of the liquid nitrogen producing line is divided into four tunnels, the liquid nitrogen runner of the first via and subcooler, upper tower liquid nitrogen into Mouth is sequentially connected, and the second tunnel is connect with the smart argon condenser inlet on pure argon column top, and third road and lower tower liquid nitrogen reflux mouth connect It connects, the 4th tunnel connects liquid nitrogen product output pipe.
Further, the rectifying section includes gas nitrogen producing line；The gas nitrogen producing line goes out from air pretreatment section dry air The mouth first via is pushed up through liquid air import, upper tower 6 in the middle part of the first feeding air of main heat exchanger runner, lower tower bottom air intlet, upper tower The supreme top of tower nitrogen outlet of portion's liquid nitrogen import；Second tunnel is through supercharger air inlet, pressurization aftercooler air inlet, main heat exchanger Second feeding air runner, expander inlet, the upper tower middle part supreme top of tower nitrogen outlet of air intlet；The gas nitrogen producing line Nitrogen outlet be directly connected to nitrogen product output channel, as output of products.
Further, first crude argon column and the second crude argon column are coupled using technique liquid argon pump.
Further, the present invention also provides the space division technique that the oxygen-enriched air separation unit of argon is mentioned using above-mentioned Full distillation, the skies Division technique includes the following steps:
1) raw air obtains through filtering, compression, cooling and after purification drying purified air, and dry purified air is divided into three Road, the first via enter main heat exchanger, with the gas converting heat that backflows, are cooled to condensing temperature, participate in rectifying into lower tower；Second tunnel Dry purified air enters main heat exchanger after pressurization is cooling and gas converting heat temperature to before expanding of backflowing, and enters back into expanding machine After refrigeration, rectifying is participated in into upper tower；The dry purified air in third road is delivered to instrument air system, as instrument supply gas and sealing Gas；
2) air is condensed and is evaporated repeatedly on multilayer column plate with reflux liquid nitrogen in rectifying section, lower tower, lower tower bottom product Poly- oxygen-enriched liquid air, oxygen-enriched liquid air are divided into two tunnels after subcooler is subcooled, and it is former as upper tower to enter upper tower top after throttling all the way Material enters crude argon condenser respectively as the tower top cold source of the first crude argon column and the second crude argon column after another way throttling, steam is made Enter upper tower for raw material；Lower column overhead nitrogen is divided into four tunnels after condenser/evaporator is condensed into liquid nitrogen, and first via liquid nitrogen is through being subcooled Upper phegma of the top of tower as upper tower is sprayed into after device supercooling, expenditure and pressure；The throttling of second road liquid nitrogen enters smart argon condenser and makees For the tower top cold source of pure argon column；Third road liquid nitrogen enters storage tank as product；4th road liquid nitrogen returns to lower tower as phegma；Under The a small amount of gas nitrogen of top of tower enters bottom heat source of the smart argon evaporator as pure argon column；
3) top of tower obtains pure nitrogen gas on, and main heat exchanger re-heat cooling box is entered after subcooler is subcooled, obtains product nitrogen Gas；Upper tower top obtains dirty nitrogen, and dirty nitrogen goes purifier conduct through subcooler supercooling, main heat exchanger re-heat cooling box, a part Regeneration gas, surplus go water-cooling tower to be vented；The product liquid oxygen of upper tower bottom enters the evaporation of main condenser evaporator, and the oxygen after evaporation is made For the upflowing vapor of upper tower, oxygen-enriched liquid air of the part liquid oxygen after cryogenic liquid pump pressurizes with lower tower bottom converges, through main heat exchange Device vaporizes re-heat cooling box, and part liquid oxygen is sent into cryogenic liquid tank as product liquid oxygen cooling box；
4) enter the first crude argon tower bottom in the thick gas argon fraction of upper tower bottom extraction, thick gas argon fraction is from the first crude argon column Bottom rises to top, subsequently into the second crude argon tower bottom, rises to top from the second crude argon tower bottom, in the process, Oxygen content in crude liquid argon fraction is lower and lower, obtains process argon at the top of the second crude argon column；Process argon is from the second crude argon tower top Portion is divided into two tunnels through conveyance conduit, enters crude argon condenser all the way, is back to the second crude argon column conduct after condensing with liquid air heat exchange Phegma, phegma to the second crude argon tower bottom are sent at the top of the first crude argon column as reflux after the pressurization of technique liquid argon pump Liquid；Another way process argon is sent into the middle part of pure argon column, and denitrification is removed in pure argon column, obtains pure liquid argon in pure argon column bottom.
From the above technical scheme, technical solution of the present invention provide a kind of Full distillation mention the oxygen-enriched air separation unit of argon and Technique, obtain it is following the utility model has the advantages that
1) present invention upper tower using pure oxygen space division technique upper tower bottom arrive liquid oxygen, liquid oxygen after liquid pump is pressurizeed with Lower tower bottom (30-40%O2) oxygen-enriched liquid air vaporizes in main heat exchanger after converging, it is changed in conjunction with oxygen-enriched space division technique, and then in master The oxygen-enriched liquid air that multiple hot medium is 80%~95% oxygen content is evaporated in hot device, compared to pure liquid oxygen, evaporating temperature is lower； It compresses in space division process inside, the more low corresponding air liquefaction temperature of the cryogenic liquid evaporating temperature backflowed is lower, and then air Condensing temperature and dew-point temperature are lower, and corresponding raw air pressure is lower, and the power consumption of corresponding air separation unit is lower；This is outside upper Tower bottom liquid oxygen converges after liquid pump is pressurizeed with lower tower bottom oxygen-enriched liquid air, is conducive to the consecutive production of single unit system, because This air separation unit of the invention is conducive to save the power consumption of air separation unit, reduces production cost.
2) tower bottom produces liquid oxygen on, crude liquid argon in oxygen-enriched liquid air can be separated with liquid oxygen, be conducive to pure argon column and mention argon, Upper tower bottom produces the oxygen-enriched liquid air of oxygen-enriched 80%~95% oxygen content in the prior art, and argon will be blended in nothing in product oxygen rich air Method is extracted, and product argon can be extracted as conventional air separation plant by mentioning the oxygen-enriched space division technique of argon using Full distillation of the invention, is saved Process flow further decreases the production cost of enterprise, increases economic efficiency.
It should be appreciated that as long as aforementioned concepts and all combinations additionally conceived described in greater detail below are at this It can be viewed as a part of the subject matter of the disclosure in the case that the design of sample is not conflicting.
Can be more fully appreciated from the following description in conjunction with attached drawing present invention teach that the foregoing and other aspects, reality Apply example and feature.The features and/or benefits of other additional aspects such as illustrative embodiments of the invention will be below Description in it is obvious, or learnt in practice by the specific embodiment instructed according to the present invention.
Detailed description of the invention
Attached drawing is not intended to drawn to scale.In the accompanying drawings, identical or nearly identical group each of is shown in each figure It can be indicated by the same numeral at part.For clarity, in each figure, not each component part is labeled. Now, example will be passed through and the embodiments of various aspects of the invention is described in reference to the drawings, in which:
Fig. 1 is the structural diagram of the present invention.
Wherein, the specific meaning of each component are as follows:
1- air filter, 2- air compressor, 3- air cooling tower, 4- molecular sieve purifier, tower under 5-, the upper tower of 6-, 7- are cold Solidifying evaporator, 8- main heat exchanger, 9- are pressurized aftercooler, 10- supercharger, 11- expanding machine, 12- subcooler, the first crude argon of 13- Tower, the second crude argon column of 14-, 15- pure argon column, 16- technique liquid argon pump, 17- crude argon condenser, 18- liquid pump, the evaporation of 19- essence argon Device, 20- essence argon condenser.
Specific embodiment
In order to better understand the technical content of the present invention, special to lift specific embodiment and institute's accompanying drawings is cooperated to be described as follows.
Various aspects with reference to the accompanying drawings to describe the present invention in the disclosure, shown in the drawings of the embodiment of many explanations. It is not intended to cover all aspects of the invention for embodiment of the disclosure.It should be appreciated that a variety of designs and reality presented hereinbefore Those of apply example, and describe in more detail below design and embodiment can in many ways in any one come it is real It applies, this is because conception and embodiment disclosed in this invention are not limited to any embodiment.In addition, disclosed by the invention one A little aspects can be used alone, or otherwise any appropriately combined use with disclosed by the invention.
Based in the prior art, on the one hand the power consumption of its operation of existing air separation plant is high, problem at high cost, another party The oxygen-enriched air separation plant of face routine obtains the pure air-liquid nitrogen of byproduct, but can not produce simultaneously pure while obtaining oxygen rich air Gas oxygen or pure liquid oxygen, the phenomenon that can not also producing gas or liquid argon simultaneously, the present invention proposes that a kind of Full distillation proposes the oxygen-enriched space division of argon Device had both been taken into account using this technique in conjunction with oxygen-enriched space division and pure oxygen space division and oxygen enriched liquid low temperature evaporation low power consumption is prepared Advantage, and take into account the advantage that liquid argon product is extracted as conventional space division.
Shown in reference to the accompanying drawing, the oxygen-enriched air separation unit of argon is mentioned to Full distillation of the invention and is further specifically introduced.
In conjunction with Fig. 1, Full distillation of the invention mentions the oxygen-enriched air separation unit of argon, including air pretreatment section, rectifying section and smart argon Section.
The air pretreatment section includes the air filter 1 being sequentially connected, air compressor 2, air cooling tower 3 and molecular sieve Purifier 4, the air pretreatment section be used to the dry removal of impurities of raw air obtaining dry purified air；Raw air is through sky Air filter 1 removes dust and mechanical admixture, and the pressure that required technical process needs is compressed in air compressor 2, pressure Contracting air is cooling through air cooling tower 3, subsequently into the molecular sieve purifier 4 of automatic switchover, for remove H2O、CO2And C2H2, with And other hydrocarbons, the temperature for the drying purified air that the molecular sieve purifier 4 exports are 15~25 DEG C.
The rectifying section includes lower tower 5, upper tower 6, condenser/evaporator 7, main heat exchanger 8, pressurization aftercooler 9, supercharger 10, expanding machine 11, subcooler 12 and liquid pump 18；The condenser/evaporator 7 is arranged between lower tower 5 and upper tower 6；The essence argon Section includes the first crude argon column 13, the second crude argon column 14, pure argon column 15, liquid argon pump 16, crude argon condenser 17, smart 19 and of argon evaporator Smart argon condenser 20.
The drying purified air outlet of above-mentioned molecular sieve purifier 4 is divided into three tunnels, and the dry purified air of the first via is changed with master Hot 8 first feeding air runner of device, the 5 bottom air import of lower tower are sequentially connected, and the dry purified air passes through main heat exchanger 8 With the gas converting heat that backflows, it is cooled to condensing temperature, participates in rectifying into lower tower 5；The dry purified air in second road and supercharger 10 air inlets, pressurization 9 air inlet of aftercooler, 8 second feeding air runner of main heat exchanger, 11 air inlet of expanding machine and upper tower 6 Middle part air intlet is sequentially connected, and the pressurization of supercharger 10, the pressurization cooling of aftercooler 9 coaxially dragged by expanding machine 11 is laggard Enter main heat exchanger 8 and the gas converting heat that backflows, be cooled to temperature before expansion, produces air separation plant into expanding machine 11 and operate normally Required cooling capacity, the dry purified air in the second road after expansion enter upper tower 6 and participate in rectifying；Third road and instrument air system into Port connection, the dry purified air in third road is as instrument supply gas and blanket gas.
The rectifying section further includes the gentle nitrogen producing line of liquid nitrogen producing line in addition to producing oxygen-enriched liquid air；The dry purifying in lower tower 5 Air at nitrogen and oxygen-enriched liquid air, obtains pure nitrogen gas in tower top by initial gross separation, and nitrogen is condensed the condensation of the liquid oxygen in evaporator 7 At liquid nitrogen；The liquid nitrogen outlet of the condenser/evaporator 7 is divided into four tunnels, the first via and the liquid nitrogen runner of subcooler 12, the liquid of upper tower 6 Nitrogen inlet is sequentially connected, and the liquid nitrogen of the first via sprays at the top of upper tower 6 after the supercooling of subcooler 12, first throttle valve decompression as upper The phegma of tower 6；Second tunnel is connect with smart 20 inlet of argon condenser on 15 top of pure argon column, and liquid nitrogen subtracts by second throttle It is pressed into the tower top cold source into smart argon condenser 20 as pure argon column 15；Third road is connect with lower 5 liquid nitrogen reflux mouth of tower, third road Liquid nitrogen returns to lower tower 5, the phegma as lower tower 5；4th tunnel connects liquid nitrogen product output pipe, is delivered to storage tank as product Storage.
The gas nitrogen producing line of the rectifying section from air pretreatment section dry air export the first via through main heat exchanger 8 first into Expect air flow channel, the 5 bottom air import of lower tower, the 6 middle part liquid air import of upper tower, the supreme 6 top nitrogen of tower of 6 top liquid nitrogen import of upper tower Gas outlet；Second tunnel through 10 air inlet of supercharger, pressurization 9 air inlet of aftercooler, 8 second feeding air runner of main heat exchanger, Supreme 6 top nitrogen of the tower outlet of 11 air inlet of expanding machine, 6 middle part air intlet of upper tower；The nitrogen outlet of the gas nitrogen producing line is straight Nitrogen product output channel is connect in succession, as output of products.
Further combined with specific embodiment, the liquid nitrogen of the condenser/evaporator 7 exports liquid nitrogen stream of the first via through subcooler Between road and the liquid nitrogen import of upper tower 6, it is provided with first throttle valve；The liquid nitrogen of the condenser/evaporator 7 exports the second tunnel and essence Second throttle is provided between smart 20 inlet of argon condenser on 15 top of argon column；The oxygen-enriched liquid air of 5 bottom of lower tower One way outlet is provided with third throttling between the oxygen-enriched liquid air import by 6 top of oxygen-enriched liquid air runner and upper tower of cooler 12 Valve；The second way outlet of oxygen-enriched liquid air of 5 bottom of lower tower through the oxygen-enriched liquid air runner of subcooler 12 and crude argon condenser 17 into The 4th throttle valve is provided between liquid mouth.
The nitrogen outlet at 5 top of the lower tower is divided into two tunnels, the smart argon evaporator 19 of the first via and 15 lower part of pure argon column into Port connection, a small amount of nitrogen enter bottom heat source of the smart argon evaporator 19 as pure argon column 15, the second tunnel and condenser/evaporator 7 Air inlet connection.
The oxygen-enriched liquid air outlet of 5 bottom of lower tower is divided into two tunnels after connecting with the oxygen-enriched liquid air runner of subcooler 12, the It is connect all the way with the oxygen-enriched liquid air import on upper 6 top of tower, the oxygen-enriched liquid air of the first via enters upper tower 6 after the decompression of third throttle valve Top, the raw material as upper tower 6；Second tunnel is connect with 17 inlet of crude argon condenser, and the oxygen-enriched liquid air on the second tunnel passes through the 4th Throttle valve decompression enters crude argon condenser 17, oxygen-enriched respectively as the tower top cold source of the first crude argon column 13 and the second crude argon column 14 The steam of liquid air enters upper tower 6 as raw material.
The drying purified air of the upper tower 6 passes through secondary rectifying, obtains purity nitrogen, and 6 top of upper tower at the top of upper tower 6 Purity nitrogen outlet be sequentially connected with the purity nitrogen runner of subcooler 12, the purity nitrogen runner of main heat exchanger 8, product nitrogen gas output channel, Purity nitrogen vaporizes re-heat cooling box through subcooler 12, main heat exchanger 8, is directly sent by pipeline with gas point or storage as product nitrogen gas Tank.
6 bottom of upper tower is connect with condenser/evaporator 7, upper 6 bottom of tower by pure oxygen air separation process obtain pure liquid oxygen into Enter the evaporation of condenser/evaporator 7, upflowing vapor of the oxygen as upper tower 6 after evaporation, the outlet of liquid oxygen autocondensation evaporator 7 is divided into two Road, the first via connect pure liquid oxygen product conveyance conduit as product liquid oxygen, the second tunnel and liquid pump 18,5 bottom of lower tower it is oxygen-enriched Liquid air outlet is sequentially connected, purity 30-40%O of the second road liquid oxygen after the pressurization of cryogenic liquid pump 18 with lower 5 bottom of tower2It is oxygen-enriched Liquid air converges, and forms oxygen-enriched air separation process, and the liquid after converging is connect with 8 liquid oxygen of main heat exchanger evaporation runner, through main heat exchanger 8 The oxygen-enriched liquid air cooling box that re-heat is 80~95% oxygen content of purity is vaporized, substantially reduces air liquefaction temperature in system, in turn So that air liquefaction temperature and dew-point temperature reduce, then the raw air pressure corresponding to it is lower, the electricity of corresponding air separation unit Consume lower, reduction production cost.
In some embodiments, above-mentioned first via liquid oxygen may also pass through 8 re-heat cooling box of main heat exchanger, produce as oxygen Product output storage, further increases and enriches the byproduct that whole Full distillation proposes the oxygen-enriched space division technique process of argon.
Dirty nitrogen, the dirt of the dirt nitrogen outlet and dirty the nitrogen runner, main heat exchanger 8 of subcooler 12 are also obtained on upper 6 top of tower Nitrogen runner is sequentially connected, and two tunnels are divided into after vaporizing re-heat cooling box, and the first via is connect with dirty nitrogen output channel, the first via Dirty nitrogen is vented by output channel in water-cooling tower；Second tunnel is connect with purifier dirt nitrogen inlet, as regeneration gas.
It is pushed up with the 13 bottom argon fraction import of the first crude argon column, the first crude argon column 13 the argon fraction outlet of 6 lower part of upper tower The thick gas argon outlet in portion and the thick gas argon import in 14 bottom of the second crude argon column are sequentially connected, i.e., extract the 7- of amount containing argon out in upper 6 lower part of tower 12% thick gas argon fraction enters 13 bottom of the first crude argon column, and thick gas argon fraction rises to top from 13 bottom of the first crude argon column Portion rises to top, in the process, crude argon fraction from 14 bottom of the second crude argon column subsequently into 14 bottom of the second crude argon column In oxygen content it is lower and lower, obtained at the top of the second crude argon column 14 oxygen content be not more than 1.5PPm process argon.
First crude argon column 13 and the second crude argon column 14 are coupled by technique liquid argon pump 16, the first crude argon column 13 and the second crude argon The cold source of tower 14 comes from low pressure liquid air evaporation endothermic；Wherein, theoretically the first crude argon column 13 and the second crude argon column 14 should be belonged to The same equipment, but the first crude argon column 13 and 14 combined altitudes of the second crude argon column are excessively high in the actual production process, are unfavorable for Production and assembly construction are so be divided into individual two crude argon columns, two crude argon column withdrawing fluid technique liquid argon pumps 16 from second 14 bottom of crude argon column is sent to the top of the first crude argon column 13, thus by the first crude argon column 13 and the second crude argon column 14 be coupled into it is similar with One equipment realizes crude argon purification process.
The process argon outlet at second crude argon column, 14 top is divided into two tunnels, the first via and 17 process argon of crude argon condenser into Mouth and 14 crude argon refluxing opening of the second crude argon column are sequentially connected, and process argon enters crude argon condenser 17, with after liquid air heat exchange condensation times The second crude argon column 14 is flow to as phegma, phegma to 14 bottom of the second crude argon column is sent again after the pressurization of technique liquid argon pump 16 Enter at the top of the first crude argon column 14 as phegma；Second tunnel is connect with the process argon import at 15 middle part of pure argon column, and in pure argon column Denitrification is removed in 15, obtains the pure liquid argon that nitrogen content is not more than 4PPm in 15 bottom of pure argon column, and the cold source at 15 top of pure argon column comes It is evaporated from low pressure liquid nitrogen, heat source is evaporated from the condensation of lower 6 top section gas nitrogen of tower in 15 bottom of pure argon column.
The pure liquid argon outlet of 15 bottom of pure argon column connects pure liquid argon product conveyance conduit；20 gas of essence argon condenser Nitrogen converges with the outlet of upper 6 top dirt nitrogen of tower to be connect with the dirty nitrogen runner of subcooler 12, main heat exchanger 8；Second crude argon column 14 The crude liquid argon outlet of bottom is connect with 16 import of liquid pump, is connect with the 13 top crude liquid argon import of the first crude argon column, under upper tower 6 The argon fraction in portion, which flows back, to be connected.
Full distillation of the invention is oxygen-enriched to propose argon technical process, and air flows into rectifying section by air pretreatment section and mentions argon Section, compared to the prior art in air separation unit greatly reduce the consumption of electricity in device production preparation process, and product kind Class is more, is conducive to enterprise's consecutive production, and reduces enterprise's production cost, improves Business Economic Benefit.
Although the present invention has been disclosed as a preferred embodiment, however, it is not to limit the invention.Skill belonging to the present invention Has usually intellectual in art field, without departing from the spirit and scope of the present invention, when can be used for a variety of modifications and variations.Cause This, the scope of protection of the present invention is defined by those of the claims.

Claims (9)

1. a kind of Full distillation mentions the oxygen-enriched air separation unit of argon, including air pretreatment section, the air pretreatment section be used to prepare Dry purified air is transmitted to rectifying section；It is characterized in that, further including rectifying section and proposing argon section；
The rectifying section include lower tower (5), upper tower (6), condenser/evaporator (7), main heat exchanger (8), pressurization aftercooler (9), Supercharger (10), expanding machine (11), subcooler (12) and liquid pump (18)；The condenser/evaporator (7) setting in Xia Ta (5) and Between upper tower (6)；
The argon section that mentions includes that the first crude argon column (13), the second crude argon column (14), pure argon column (15), liquid pump (16), crude argon are cold Condenser (17), smart argon evaporator (19) and smart argon condenser (20)；
The dry purified air outlet of the air pretreatment section is divided into three tunnels, the first via and (8) first feeding air of main heat exchanger Runner, lower tower (5) bottom air import are sequentially connected, the second tunnel and supercharger (10) air inlet, pressurization aftercooler (9) air inlet Air intlet is sequentially connected in the middle part of mouth, (8) second feeding air runner of main heat exchanger, expanding machine (11) air inlet and upper tower (6), Third road is connect with instrument air system air inlet；
Nitrogen outlet at the top of the lower tower (5) is divided into two tunnels, and the first via is connect with condenser/evaporator (7) air inlet；Second tunnel It is connect with smart argon evaporator (19) air inlet of pure argon column (15) lower part；
The oxygen-enriched liquid air outlet of lower tower (5) bottom is divided into two tunnels after connecting with the oxygen-enriched liquid air runner of subcooler (12), the It is connect all the way with the oxygen-enriched liquid air import on upper tower (6) top, the second tunnel is connect with crude argon condenser (17) inlet；
Condenser/evaporator (7) the liquid nitrogen runner exit is divided into two tunnels, and the liquid nitrogen reflux mouth at the top of the first via and lower tower (5) connects It connects, the second tunnel is connect with the liquid nitrogen runner of subcooler (12)；
The liquid nitrogen runner exit of the subcooler (12) is divided into three tunnels, and the first via is connect with liquid nitrogen reflux mouth at the top of upper tower (6), the Two tunnels connect pure liquid nitrogen product conveyance conduit, third Lu Yujing argon condenser (20) liquid nitrogen import connection as nitrogen products；
Upper tower (6) bottom is connect with condenser/evaporator (7), and the liquid oxygen of upper tower (6) bottom enters condenser/evaporator (7), liquid Oxygen autocondensation evaporator (7) outlet is divided into two tunnels, and the first via connects pure liquid oxygen product conveyance conduit, the second tunnel as product liquid oxygen Oxygen-enriched liquid air outlet with liquid pump (18), lower tower (5) bottom is sequentially connected, the liquid after converging and main heat exchanger (8) liquid oxygen Evaporate runner connection；
The dirty nitrogen outlet on upper tower (6) top is connect with the dirty nitrogen runner of subcooler (12), main heat exchanger (8)；
Purity nitrogen outlet at the top of the upper tower (6) is connect with the purity nitrogen runner of subcooler (12), main heat exchanger (8)；
The outlet of argon fraction and the argon fraction import of the first crude argon column (13) bottom, the first crude argon column (13) of upper tower (6) lower part The thick gas argon outlet in top and the thick gas argon import in the second crude argon column (14) bottom are sequentially connected；
Process argon outlet at the top of second crude argon column (14) is divided into two tunnels, the first via and crude argon condenser (17) process argon into Mouth and the second crude argon column (14) crude argon refluxing opening are sequentially connected, and the second tunnel is connect with the process argon import in the middle part of pure argon column (15)；
The pure liquid argon outlet of pure argon column (15) bottom connects pure liquid argon product conveyance conduit；
Essence argon condenser (20) the gas nitrogen and the outlet of upper tower (6) top dirt nitrogen converge and subcooler (12), main heat exchanger (8) Dirty nitrogen runner connection；
The crude liquid argon outlet of second crude argon column (14) bottom is connect with liquid pump (16) import, is pushed up with the first crude argon column (13) Crude liquid argon import connection in portion's flows back with the argon fraction of upper tower (6) lower part and connects.
2. Full distillation according to claim 1 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the air pretreatment section packet Include the air filter (1) being sequentially connected, air compressor (2), air cooling tower (3) and molecular sieve purifier (4)；The air is pre- Processing section be used to the dry removal of impurities of raw air obtaining dry purified air, and be transmitted to rectifying section rectification and purification.
3. Full distillation according to claim 1 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the rectifying section includes liquid nitrogen Producing line；
The liquid nitrogen producing line is exported from air pretreatment section dry air through (8) first feeding air runner of main heat exchanger, lower tower (5) bottom air import, the outlet of lower tower (5) top nitrogen, condenser/evaporator (7) nitrogen inlet to condenser/evaporator (7) liquid nitrogen Outlet.
4. Full distillation according to claim 3 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the liquid nitrogen of the liquid nitrogen producing line Outlet be divided into four tunnels, the first via and the liquid nitrogen import of the liquid nitrogen runner, upper tower (6) of subcooler (12) are sequentially connected, the second tunnel and Smart argon condenser (2) inlet on pure argon column (15) top connects, and third road is connect with lower tower (5) liquid nitrogen reflux mouth, the 4th tunnel Connect liquid nitrogen product output pipe.
5. Full distillation according to claim 1 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the rectifying section includes gas nitrogen Producing line；
The gas nitrogen producing line is from the air pretreatment section dry air outlet first via through (8) first feed air stream of main heat exchanger Road, lower tower (5) bottom air import, the liquid air import of upper tower (6) middle part, upper tower (6) the top supreme tower of liquid nitrogen import (6) top nitrogen Gas outlet；Second tunnel is through supercharger (10) air inlet, pressurization aftercooler (9) air inlet, (8) second feeding air of main heat exchanger Runner, expanding machine (11) air inlet, air intlet supreme tower (6) the top nitrogen outlet of upper tower (6) middle part.
6. Full distillation according to claim 5 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the nitrogen of the gas nitrogen producing line Outlet is directly connected to nitrogen product output channel.
7. Full distillation according to claim 1 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the first crude argon column (13) and Two crude argon columns (14) are coupled using technique liquid argon pump (16).
8. Full distillation according to claim 4 mentions the oxygen-enriched air separation unit of argon, which is characterized in that the condenser/evaporator (7) Liquid nitrogen outlet liquid nitrogen runner of the first via through subcooler and the liquid nitrogen import of upper tower (6) between, be provided with first throttle valve；Institute The liquid nitrogen for stating condenser/evaporator (7) exports to be arranged between the second tunnel and smart argon condenser (20) inlet on pure argon column (15) top There is second throttle；The first way outlet of oxygen-enriched liquid air of lower tower (5) bottom by cooler (12) oxygen-enriched liquid air runner with Third throttle valve is provided between the oxygen-enriched liquid air import on upper tower (6) top；The second tunnel of oxygen-enriched liquid air of lower tower (5) bottom It exports the oxygen-enriched liquid air runner through subcooler (12) and is provided with the 4th throttle valve between crude argon condenser (17) inlet.
9. a kind of Full distillation mentions the oxygen-enriched space division technique of argon, which is characterized in that air separation unit described in claim 1 is used, including Following steps:
1) raw air obtains through filtering, compression, cooling and after purification drying purified air, and dry purified air is divided into three tunnels, The first via enters main heat exchanger (8) and is cooled to condensing temperature with the gas converting heat that backflows, and participates in rectifying into lower tower (5)；The The dry purified air in two roads enters main heat exchanger (8) after pressurization is cooling and gas converting heat temperature to before expanding of backflowing, then into After entering expanding machine (11) refrigeration, rectifying is participated in into upper tower (6)；The dry purified air in third road is delivered to instrument air system, As instrument supply gas and blanket gas；
2) in rectifying section, the interior air of lower tower (5) is condensed and is evaporated repeatedly on multilayer column plate with reflux liquid nitrogen, lower tower (5) bottom Oxygen-enriched liquid air is gathered, oxygen-enriched liquid air is divided into two tunnels after subcooler (12) are subcooled, and enters upper tower (6) top after throttling all the way and makees For upper tower (6) raw material, enters crude argon condenser (17) after another way throttling and be used as the first crude argon column (13) and the second crude argon column (14) tower top cold source, steam enter upper tower (6) as raw material；Lower tower (5) nitrogen overhead is condensed into liquid through condenser/evaporator (7) It is divided into four tunnels after nitrogen, first via liquid nitrogen is subcooled through subcooler (12), is sprayed at the top of upper tower (6) after expenditure and pressure as upper tower (6) Phegma；The throttling of second road liquid nitrogen enters tower top cold source of the smart argon condenser (20) as pure argon column (15)；Third road liquid nitrogen Enter storage tank as product；4th road liquid nitrogen returns to lower tower (5) and is used as phegma；The lower a small amount of gas nitrogen of top of tower enters smart argon evaporation Bottom heat source of the device as pure argon column (15)；
3) pure nitrogen gas is obtained at the top of tower (6) on, enters main heat exchanger (8) re-heat cooling box after subcooler (12) supercooling, obtains Product nitrogen gas；Upper tower (6) top obtains dirty nitrogen, and dirty nitrogen is subcooled through subcooler (12), main heat exchanger (8) re-heat cooling box, A part goes purifier as regeneration gas, and surplus goes water-cooling tower to be vented；The product liquid oxygen of upper tower (6) bottom enters main condenser evaporation Device (7) evaporation, upflowing vapor of the oxygen as upper tower (6) after evaporation, part liquid oxygen through cryogenic liquid pump (18) pressurize after with The oxygen-enriched liquid air of lower tower bottom converges, and vaporizes re-heat cooling box through main heat exchanger (8), part liquid oxygen enters storage tank as product；
4) enter the first crude argon column (13) bottom in the thick gas argon fraction of (6) bottom Shang Ta extraction, thick gas argon fraction is thick from first Argon column (13) bottom rises to top, subsequently into the second crude argon column (14) bottom, rises to from the second crude argon column (14) bottom Top, in the process, the oxygen content in crude liquid argon fraction are lower and lower, obtain process argon at the top of the second crude argon column (14)； Process argon is divided into two tunnels through conveyance conduit from the top of the second crude argon column (14), enters crude argon condenser (17) all the way, changes with liquid air The second crude argon column (14) are back to after heat condensation as phegma, phegma to the second crude argon column (14) bottom passes through technique liquid argon It is sent into after pump (16) pressurization at the top of the first crude argon column (14) as phegma；Another way process argon is sent into the middle part of pure argon column (15), Denitrification is removed in pure argon column (15), obtains pure liquid argon in pure argon column (15) bottom.
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CN115839600A (en) * 2023-02-22 2023-03-24 中科富海(杭州)气体工程科技有限公司 Cryogenic air separation device

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