CN109186179B - Full-rectification argon extraction oxygen-enriched air separation device and process - Google Patents

Full-rectification argon extraction oxygen-enriched air separation device and process Download PDF

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Publication number
CN109186179B
CN109186179B CN201811154245.4A CN201811154245A CN109186179B CN 109186179 B CN109186179 B CN 109186179B CN 201811154245 A CN201811154245 A CN 201811154245A CN 109186179 B CN109186179 B CN 109186179B
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tower
argon
liquid
air
oxygen
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CN109186179A (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
    • F25J3/04763—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
    • F25J3/04406—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
    • F25J3/04006—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
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
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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
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    • 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)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention provides a full-rectification argon-extracting oxygen-enriched air separation device, which relates to the field of air separation equipment and comprises an air pretreatment section, a rectification section and an argon rectification section; the rectifying section comprises a lower tower, an upper tower, a condensing evaporator, a main heat exchanger, a booster compressor/expander, a post-booster cooler and a subcooler, wherein an oxygen-enriched liquid air outlet at the bottom of the lower tower is connected with an oxygen-enriched liquid air flow passage of the subcooler and then is divided into two paths, and the two paths are connected with an oxygen-enriched liquid air inlet of the upper tower and a liquid inlet of a crude argon condenser; the liquid oxygen at the bottom of the upper tower enters a condensation evaporator, the outlet of the self-condensation evaporator is divided into two paths, one path is used as product liquid oxygen to be connected with a pure liquid oxygen product conveying pipeline, and the other path is sequentially connected with a liquid pump and an oxygen-enriched liquid air outlet at the bottom of the lower tower; the argon fraction at the lower part of the upper tower sequentially passes through a first crude argon tower, a second crude argon tower and a refined argon tower to obtain pure liquid argon; the invention has the advantages that the argon is extracted by the oxygen-enriched air separation device, the product variety of the device is increased, and the economic benefit is improved.

Description

Full-rectification argon extraction oxygen-enriched air separation device and process
Technical Field
The invention relates to the field of cryogenic air separation equipment, in particular to a full-rectification argon-extracting oxygen-enriched air separation device and a full-rectification argon-extracting oxygen-enriched air separation process.
Background
Air refers to a mixture of gases in the earth's atmosphere consisting essentially of 78% nitrogen, 21% oxygen, 0.94% noble gases (helium, neon, argon, krypton, xenon), 0.03% carbon dioxide, 0.03% other substances (e.g., water vapor, impurities, etc.), wherein the noble gases are essentially argon components.
The air separation equipment is equipment which takes air as a raw material, turns the air into liquid state by a compression circulation deep freezing method, and gradually separates and produces inert gases such as oxygen, nitrogen, argon and the like from the liquid air by rectification. The air separation equipment is a large complex system and mainly comprises a power system, a purifying system, a refrigerating system, a heat exchange system, a rectifying system, a product conveying system, a liquid storage system, a control system and the like.
The power system mainly refers to an air compressor, air is separated by air separation equipment at low temperature to obtain products such as oxygen, nitrogen and the like, the energy conversion is essentially completed, and the energy of the device is mainly input by the air compressor; the purification system consists of an air pre-cooling system and a molecular sieve purification system, wherein the temperature of the compressed raw material air is higher, the air pre-cooling system can reduce the temperature of the air through contact heat exchange, and meanwhile, harmful impurities such as acidic substances and the like in the air can be washed, and the molecular sieve purification system can further remove substances such as moisture, carbon dioxide, acetylene, propylene, propane, nitrous oxide and the like in the air, which are harmful to the operation of air equipment; the refrigerating system of the air separation equipment is realized through an expander, and the refrigeration of the whole air separation equipment strictly follows classical refrigeration cycle; the heat balance of the air separation equipment is completed by a refrigeration system and a heat exchange system, and in the prior art, an aluminum plate-fin heat exchanger is mainly used as a heat exchanger; the core of the air separation equipment is a rectification system for realizing low-temperature separation of air components, and the air separation equipment consists of a low-pressure tower, a medium-pressure tower and a condensation evaporator; the oxygen and the nitrogen produced by the air separation equipment can meet the requirement of the subsequent system by a certain pressure, and are completed through each pipeline of the product conveying system; products such as liquid oxygen, liquid nitrogen and the like produced by the air separation equipment enter a liquid storage system; the existing large-scale air separation equipment adopts a computer distributed control system to realize automatic control.
The main products of the equipment are liquid nitrogen, liquid oxygen and oxygen-enriched air, and the oxygen-enriched air is mainly applied to combustion supporting of steelmaking furnaces, glass furnaces, metal smelting and the like. The pressure required by oxygen-enriched air for combustion supporting is generally 0.1-0.2MPa. The conventional oxygen-enriched air separation equipment adopts double-stage rectification, oxygen-enriched gas is directly obtained at the bottom of the upper tower and is pressurized to the required pressure by an oxygen compressor after being subjected to primary heat exchange and reheating, or oxygen-enriched liquid air is obtained at the bottom of the upper tower, and is compressed by a liquid oxygen pump or is subjected to self-pressurization to the required pressure and is subjected to reheating and then is discharged out of a fractionating tower cold box.
The existing refrigeration system of the air separation equipment consumes a large amount of electric energy due to the dew point of each gas which needs to be reached, so that the production cost is increased; in addition, the conventional oxygen-enriched air separation equipment can produce byproducts of pure nitrogen and liquid nitrogen while obtaining oxygen-enriched air, can not produce pure oxygen or pure liquid oxygen at the same time, and can not produce argon or liquid argon at the same time.
Disclosure of Invention
The invention aims to provide a full-rectification argon-extracting oxygen-enriched air separation device and a full-rectification argon-extracting oxygen-enriched air separation process, which can effectively reduce the power consumption in the full-rectification argon-extracting oxygen-enriched air separation process, and simultaneously produce by-products of pure liquid nitrogen and oxygen or liquid oxygen and liquid argon or argon.
In order to achieve the above purpose, the present invention proposes the following technical scheme: an oxygen-enriched air separation device for full rectification argon extraction comprises an air pretreatment section, wherein the air pretreatment section is used for preparing dry purified air and transmitting the dry purified air to a rectification section;
the device also comprises a rectifying section and an argon extracting section, wherein the rectifying section comprises a lower tower, an upper tower, a condensing evaporator, a main heat exchanger, a post-supercharging cooler, a supercharger, an expander, a subcooler and a liquid pump; the condensing evaporator is arranged between the lower tower and the upper tower; the argon extracting section comprises a first crude argon tower, a second crude argon tower, a refined argon tower, a process liquid argon pump, a crude argon condenser, a refined argon evaporator and a refined argon condenser;
the air pretreatment section is divided into three paths, wherein the first path is sequentially connected with a first feeding air flow passage of a main heat exchanger and an air inlet at the bottom of a lower tower, the second path is sequentially connected with a supercharger air inlet, a post-supercharging cooler air inlet, a second feeding air flow passage of the main heat exchanger, an expander air inlet and an air inlet at the middle part of an upper tower, and the third path is connected with an air inlet of an instrument air system;
the nitrogen outlet at the top of the lower tower is divided into two paths, and the first path is connected with the air inlet of the condensing evaporator; the second path is connected with an air inlet of a refined argon evaporator at the lower part of the refined argon tower;
the oxygen-enriched liquid air outlet at the bottom of the lower tower is connected with the oxygen-enriched liquid air channel of the subcooler and then is divided into two paths, wherein the first path is connected with the oxygen-enriched liquid air inlet at the upper part of the upper tower, and the second path is connected with the liquid inlet of the crude argon condenser;
the outlet of the liquid nitrogen flow passage of the condensing evaporator is divided into two paths, the first path is connected with a liquid nitrogen reflux port at the top of the lower tower, and the second path is connected with a liquid nitrogen flow passage of the subcooler;
the liquid nitrogen runner outlet of the subcooler is divided into three paths, the first path is connected with a liquid nitrogen reflux port at the top of the upper tower, the second path is used as product liquid nitrogen to be connected with a pure liquid nitrogen product conveying pipeline, and the third path is connected with a liquid nitrogen inlet of the refined argon condenser;
the bottom of the upper tower is connected with the condensation evaporator, liquid oxygen at the bottom of the upper tower enters the condensation evaporator, the outlet of the liquid oxygen self-condensation evaporator is divided into two paths, the first path is used as product liquid oxygen to be connected with a pure liquid oxygen product conveying pipeline, the second path is sequentially connected with a liquid pump and an oxygen-enriched liquid air outlet at the bottom of the lower tower, and the liquid after merging is connected with a liquid oxygen evaporation flow passage of the main heat exchanger;
the dirty nitrogen at the upper part of the upper tower is connected with a dirty nitrogen runner of the subcooler and the main heat exchanger;
pure nitrogen at the top of the upper tower is connected with a pure nitrogen connecting channel of the subcooler and the main heat exchanger;
the argon fraction outlet at the lower part of the upper tower is sequentially connected with the argon fraction inlet at the bottom of the first crude argon tower, the crude gas argon outlet at the top of the first crude argon tower and the crude gas argon inlet at the bottom of the second crude argon tower;
the process argon outlet at the top of the second crude argon tower is divided into two paths, the first path is connected with the process argon inlet of the crude argon condenser and the crude argon reflux port of the second crude argon tower in sequence, and the second path is connected with the process argon inlet at the middle part of the refined argon tower;
the pure liquid argon outlet at the bottom of the refined argon tower is connected with a pure liquid argon product conveying pipeline;
the refined argon condenser gas nitrogen and a dirty nitrogen outlet at the upper part of the upper tower are converged and connected with a dirty nitrogen runner of the subcooler and the main heat exchanger;
and a crude liquid argon outlet at the bottom of the second crude argon tower is connected with an inlet of a process liquid argon pump, is connected with an inlet of crude liquid argon at the top of the first crude argon tower, and is in reflux connection with an argon fraction at the lower part of the upper tower.
Further, the rectifying section comprises a liquid nitrogen production line; the liquid nitrogen production line is from a dry air outlet of the air pretreatment section to a liquid nitrogen outlet of the condensing evaporator through a first feeding air flow passage of the main heat exchanger, an air inlet at the bottom of the lower tower, a nitrogen outlet at the top of the lower tower and a nitrogen inlet of the condensing evaporator;
the liquid nitrogen outlet of the liquid nitrogen production line is divided into four paths, the first path is sequentially connected with a liquid nitrogen runner of the subcooler and a liquid nitrogen inlet of the upper tower, the second path is connected with a liquid inlet of a refined argon condenser at the upper part of the refined argon tower, the third path is connected with a liquid nitrogen reflux port of the lower tower, and the fourth path is connected with a liquid nitrogen product output pipeline.
Further, the rectifying section comprises a gas nitrogen production line; the first path of the air nitrogen production line passes through a first feeding air flow passage of the main heat exchanger, a lower tower bottom air inlet, an upper tower middle liquid air inlet, an upper tower 6 top liquid nitrogen inlet and an upper tower top nitrogen outlet from a dry air outlet of the air pretreatment section; the second path passes through a booster air inlet, a booster post-cooler air inlet, a main heat exchanger second feeding air flow passage, an expander air inlet, an upper tower middle air inlet and an upper tower top nitrogen outlet; the nitrogen outlet of the gas nitrogen production line is directly connected with a nitrogen product output pipeline to be used as a product output.
Further, the first crude argon column and the second crude argon column are coupled using a process liquid argon pump.
Further, the invention also provides a space division process adopting the Quan Jingliu argon-extracting oxygen-enriched space division device, which comprises the following steps:
1) Raw material air is filtered, compressed, cooled and purified to obtain dry purified air, the dry purified air is divided into three paths, the first path enters a main heat exchanger to exchange heat with the reflux gas, and the dry purified air is cooled to the liquefaction temperature and enters a lower tower to participate in rectification; the second path of dry purified air enters a main heat exchanger to exchange heat with the reflux gas to reach the temperature before expansion after being pressurized and cooled, and enters an expander to be refrigerated and then enters an upper tower to participate in rectification; the third path of dry purified air is conveyed to an instrument air system to serve as instrument air and sealing air;
2) In the rectifying section, air and reflux liquid nitrogen in a lower tower are repeatedly condensed and evaporated on a plurality of layers of tower plates, oxygen-enriched liquid air is accumulated at the bottom of the lower tower, the oxygen-enriched liquid air is supercooled by a supercooler and then is divided into two paths, one path of the oxygen-enriched liquid air enters the upper part of an upper tower to be used as an upper tower raw material, the other path of the oxygen-enriched liquid air enters a crude argon condenser to be used as a tower top cold source of a first crude argon tower and a second crude argon tower respectively after being throttled, and steam enters the upper tower as a raw material; the nitrogen at the top of the lower tower is condensed into liquid nitrogen by a condensing evaporator and then divided into four paths, and the first path of liquid nitrogen is supercooled by a subcooler, throttled and decompressed and then sprayed into the top of the upper tower to be used as reflux liquid of the upper tower; the second liquid nitrogen is throttled and enters a refined argon condenser to be used as a top cold source of a refined argon tower; the third liquid nitrogen is taken as a product to enter a storage tank; the fourth liquid nitrogen returns to the lower tower to be used as reflux liquid; a small amount of gas nitrogen at the top of the lower tower enters the refined argon evaporator to be used as a bottom heat source of the refined argon tower;
3) Pure nitrogen is obtained at the top of the upper tower, and enters a main heat exchanger for reheating to obtain nitrogen product after being supercooled by a cooler; the upper part of the upper tower is provided with dirty nitrogen, the dirty nitrogen is subjected to supercooling through a cooler and re-heating through a main heat exchanger to be discharged out of a cold box, a part of the depurating device is used as regenerated gas, and the rest of the dewatering cooling tower is emptied; the product liquid oxygen at the bottom of the upper tower enters a main condensing evaporator to evaporate, the evaporated oxygen is used as rising steam of the upper tower, part of liquid oxygen is pressurized by a low-temperature liquid pump and then is merged with the oxygen-enriched liquid air at the bottom of the lower tower, the vaporized and reheated liquid oxygen is discharged out of a cold box through a main heat exchanger, and part of liquid oxygen is discharged out of the cold box as product liquid oxygen and is sent into a low-temperature liquid storage tank;
4) The crude gas argon fraction extracted from the bottom of the upper tower enters the bottom of a first crude argon tower, the crude gas argon fraction rises from the bottom of the first crude argon tower to the top, then enters the bottom of a second crude argon tower, and rises from the bottom of the second crude argon tower to the top, in the process, the oxygen content in the crude liquid argon fraction is lower and lower, and process argon is obtained from the top of the second crude argon tower; the process argon is divided into two paths from the top of the second crude argon tower through a conveying pipeline, one path enters a crude argon condenser, and flows back to the second crude argon tower as reflux liquid after being condensed by liquid-air heat exchange, and the reflux liquid is fed into the top of the first crude argon tower as reflux liquid after being pressurized by a process liquid argon pump; and the other path of process argon is sent to the middle part of the refined argon tower, nitrogen is removed in the refined argon tower, and pure liquid argon is obtained at the bottom of the refined argon tower.
According to the technical scheme, the invention provides the full-rectification argon-extracting oxygen-enriched air separation device and the full-rectification argon-extracting oxygen-enriched air separation process, and the following beneficial effects are obtained:
1) The invention adopts pure oxygen space separation technology to reach liquid oxygen at the bottom of the upper tower, and the liquid oxygen is pressurized by a liquid pump and then is connected with the bottom of the lower tower (30-40% O) 2 ) The oxygen-enriched liquid air is vaporized in the main heat exchanger after being converged, and the evaporation temperature is lower compared with pure liquid oxygen because the oxygen-enriched liquid air with 80% -95% oxygen content of the medium evaporated and reheated in the main heat exchanger is combined with an oxygen-enriched air separation process; in the internal compression air separation flow, the lower the evaporation temperature of the low-temperature liquid in the reflux is, the lower the air liquefaction temperature and the dew point temperature are, the lower the corresponding raw material air pressure is, and the lower the power consumption of the corresponding air separation device is; in addition, the liquid oxygen at the bottom of the upper tower is pressurized by a liquid pump and then is connected with the lower towerThe bottom oxygen-enriched liquid is empty to be converged, which is beneficial to the continuous production of the whole device, so that the air separation device is beneficial to saving the power consumption of the air separation device and reducing the production cost.
2) The liquid oxygen is produced at the bottom of the upper tower, so that crude liquid argon in the oxygen-enriched liquid air can be separated from liquid oxygen, the argon extraction of an argon refining tower is facilitated, the oxygen-enriched liquid air with 80% -95% oxygen content is produced at the bottom of the upper tower in the prior art, argon is mixed in the product oxygen-enriched air and cannot be extracted, and the full-rectification argon-extraction oxygen-enriched air separation process can be used for extracting the product argon as the same as conventional air separation equipment, so that the process flow is saved, the production cost of enterprises is further reduced, and the economic benefit is improved.
It should be understood that all combinations of the foregoing concepts, as well as additional concepts described in more detail below, may be considered a part of the inventive subject matter of the present disclosure as long as such concepts are not mutually inconsistent.
The foregoing and other aspects, embodiments, and features of the present teachings will be more fully understood from the following description, taken together with the accompanying drawings. Other additional aspects of the invention, such as features and/or advantages of the exemplary embodiments, will be apparent from the description which follows, or may be learned by practice of the embodiments according to the teachings of the invention.
Drawings
The drawings are not intended to be drawn to scale. In the drawings, each identical or nearly identical component that is illustrated in various figures may be represented by a like numeral. For purposes of clarity, not every component may be labeled in every drawing. Embodiments of various aspects of the invention will now be described, by way of example, with reference to the accompanying drawings, in which:
fig. 1 is a schematic structural view of the present invention.
The specific meaning of each component is as follows:
1-air filter, 2-air compressor, 3-air cooling tower, 4-molecular sieve purifier, 5-lower tower, 6-upper tower, 7-condensing evaporator, 8-main heat exchanger, 9-after-pressurization cooler, 10-booster, 11-expander, 12-subcooler, 13-first crude argon tower, 14-second crude argon tower, 15-refined argon tower, 16-process liquid argon pump, 17-crude argon condenser, 18-liquid pump, 19-refined argon evaporator, 20-refined argon condenser.
Detailed Description
For a better understanding of the technical content of the present invention, specific examples are set forth below, along with the accompanying drawings. Aspects of the invention are described in this disclosure with reference to the drawings, in which are shown a number of illustrative embodiments. The embodiments of the present disclosure are not necessarily intended to include all aspects of the invention. It should be understood that the various concepts and embodiments described above, as well as those described in more detail below, may be implemented in any of a number of ways, as the disclosed concepts and embodiments are not limited to any implementation. Additionally, some aspects of the disclosure may be used alone or in any suitable combination with other aspects of the disclosure.
Based on the problems of high power consumption and high cost of the operation of the existing air separation equipment in the prior art, on the one hand, pure gas and liquid nitrogen are obtained as byproducts while oxygen-enriched gas is obtained by the conventional oxygen-enriched air separation equipment, but pure gas oxygen or pure liquid oxygen cannot be produced simultaneously, and the phenomenon that gas or liquid argon cannot be produced simultaneously is also avoided.
The full-rectification argon-extracting oxygen-enriched air separation device is further specifically described below with reference to the accompanying drawings.
With reference to FIG. 1, the full-rectification argon-extracting oxygen-enriched air separation device comprises an air pretreatment section, a rectification section and an argon rectification section.
The air pretreatment section comprises an air filter 1, an air compressor 2, an air cooling tower 3 and a molecular sieve purifier 4 which are sequentially connected, and is used for drying raw material air and removing impurities to obtain dry purified air; raw air is filtered by an air filter 1 to remove dust and mechanical impurities, and compressed in an air compressor 2 to a desired processThe compressed air is cooled by an air cooling tower 3 and then enters an automatically switched molecular sieve purifier 4 for removing H 2 O、CO 2 And C 2 H 2 And other hydrocarbons, the temperature of the dry purified air at the outlet of the molecular sieve purifier 4 is 15 to 25 ℃.
The rectifying section comprises a lower tower 5, an upper tower 6, a condensing evaporator 7, a main heat exchanger 8, a post-pressurizing cooler 9, a pressurizing machine 10, an expansion machine 11, a subcooler 12 and a liquid pump 18; the condensing evaporator 7 is arranged between the lower tower 5 and the upper tower 6; the refined argon section comprises a first crude argon column 13, a second crude argon column 14, a refined argon column 15, a process liquid argon pump 16, a crude argon condenser 17, a refined argon evaporator 19 and a refined argon condenser 20.
The drying and purifying air outlet of the molecular sieve purifier 4 is divided into three paths, the first path of drying and purifying air is sequentially connected with a first feeding air flow passage of the main heat exchanger 8 and an air inlet at the bottom of the lower tower 5, and the drying and purifying air exchanges heat with the reflux gas through the main heat exchanger 8 and is cooled to the liquefaction temperature and enters the lower tower 5 to participate in rectification; the second path of dry purified air is sequentially connected with an air inlet of a booster 10, an air inlet of a post-booster cooler 9, a second feeding air flow passage of a main heat exchanger 8, an air inlet of an expander 11 and an air inlet in the middle of an upper tower 6, the booster 10 coaxially dragged by the expander 11 boosts the pressure, the post-booster cooler 9 cools the air and then enters the main heat exchanger 8 to exchange heat with the reflux gas, the air is cooled to the temperature before expansion, the air enters the expander 11 to prepare the cold energy required by the normal operation of air separation equipment, and the expanded second path of dry purified air enters the upper tower 6 to participate in rectification; the third path is connected with an air inlet of the instrument air system, and the third path of dry purified air is used as instrument air and sealing air.
The rectifying section comprises a liquid nitrogen production line and a gas nitrogen production line besides the production of the oxygen-enriched liquid air; the dry purified air is primarily separated into nitrogen and oxygen-enriched liquid air in a lower tower 5, pure nitrogen is obtained at the top of the tower, and the nitrogen is condensed into liquid nitrogen by liquid oxygen in a condensing evaporator 7; the liquid nitrogen outlet of the condensing evaporator 7 is divided into four paths, the first path is sequentially connected with a liquid nitrogen flow passage of the subcooler 12 and a liquid nitrogen inlet of the upper tower 6, and liquid nitrogen of the first path is subcooled by the subcooler 12 and is depressurized by a first throttle valve and then sprayed into the top of the upper tower 6 to be used as reflux liquid of the upper tower 6; the second path is connected with a liquid inlet of a refined argon condenser 20 at the upper part of the refined argon tower 15, and liquid nitrogen enters the refined argon condenser 20 through a second throttle valve in a decompression way to serve as a top cold source of the refined argon tower 15; the third path is connected with a liquid nitrogen reflux port of the lower tower 5, and the liquid nitrogen of the third path returns to the lower tower 5 to be used as reflux liquid of the lower tower 5; the fourth path is connected with a liquid nitrogen product output pipeline and is used as a product to be conveyed to a storage tank for storage.
The gas nitrogen production line of the rectifying section passes through a first feeding air flow passage of the main heat exchanger 8 from a first dry air outlet of the air pretreatment section, an air inlet at the bottom of the lower tower 5, a liquid air inlet in the middle of the upper tower 6, a liquid nitrogen inlet at the top of the upper tower 6 and a nitrogen outlet at the top of the upper tower 6; the second path passes through a supercharger 10 air inlet, a supercharged aftercooler 9 air inlet, a second feeding air flow passage of the main heat exchanger 8, an expander 11 air inlet, an upper tower 6 middle air inlet and an upper tower 6 top nitrogen outlet; the nitrogen outlet of the gas nitrogen production line is directly connected with a nitrogen product output pipeline to be used as a product output.
Further combining with the specific embodiment, a first throttle valve is arranged between the liquid nitrogen flow passage of the condenser-evaporator 7 and the liquid nitrogen inlet of the upper tower 6; a second throttle valve is arranged between a liquid nitrogen outlet second path of the condensation evaporator 7 and a liquid inlet of the refined argon condenser 20 at the upper part of the refined argon tower 15; a third throttle valve is arranged between an oxygen-enriched liquid air channel of the oxygen-enriched liquid air outlet at the bottom of the lower tower 5 passing through the subcooler 12 and an oxygen-enriched liquid air inlet at the upper part of the upper tower 6; a fourth throttle valve is arranged between an oxygen-enriched liquid air flow passage of the oxygen-enriched liquid air outlet at the bottom of the lower tower 5 through the cooler 12 and a liquid inlet of the crude argon condenser 17.
The nitrogen outlet at the top of the lower tower 5 is divided into two paths, the first path is connected with the air inlet of the refined argon evaporator 19 at the lower part of the refined argon tower 15, a small amount of nitrogen enters the refined argon evaporator 19 to serve as a bottom heat source of the refined argon tower 15, and the second path is connected with the air inlet of the condensation evaporator 7.
The oxygen-enriched liquid air outlet at the bottom of the lower tower 5 is connected with the oxygen-enriched liquid air flow passage of the subcooler 12 and then is divided into two paths, the first path is connected with the oxygen-enriched liquid air inlet at the upper part of the upper tower 6, and the oxygen-enriched liquid air of the first path enters the upper part of the upper tower 6 after being depressurized through a third throttling valve and is used as a raw material of the upper tower 6; the second path is connected with a liquid inlet of the crude argon condenser 17, oxygen-enriched liquid air in the second path is decompressed and enters the crude argon condenser 17 through a fourth throttle valve, and the oxygen-enriched liquid air is respectively used as a top cold source of the first crude argon tower 13 and the second crude argon tower 14, and steam of the oxygen-enriched liquid air is used as a raw material and enters the upper tower 6.
The dry purified air of the upper tower 6 is subjected to secondary rectification to obtain pure nitrogen at the top of the upper tower 6, a pure nitrogen outlet at the top of the upper tower 6 is sequentially connected with a pure nitrogen flow passage of the subcooler 12, a pure nitrogen flow passage of the main heat exchanger 8 and a product nitrogen output pipeline, and the pure nitrogen is vaporized and reheated by the subcooler 12 and the main heat exchanger 8 to form a cold box, and is used as product nitrogen to be directly sent to a gas point or a storage tank through the pipeline.
The bottom of the upper tower 6 is connected with a condensation evaporator 7, pure liquid oxygen obtained from the bottom of the upper tower 6 through a pure oxygen air separation process enters the condensation evaporator 7 for evaporation, the evaporated oxygen is used as rising steam of the upper tower 6, the liquid oxygen is divided into two paths from an outlet of the condensation evaporator 7, the first path is used as product liquid oxygen to be connected with a pure liquid oxygen product conveying pipeline, the second path is sequentially connected with a liquid pump 18 and an oxygen-enriched liquid air outlet at the bottom of the lower tower 5, and the second path of liquid oxygen is pressurized by the low-temperature liquid pump 18 and then is connected with the purity of 30-40% O at the bottom of the lower tower 5 2 The oxygen-enriched liquid air is converged to form an oxygen-enriched air separation process, the converged liquid is connected with a liquid oxygen evaporation flow passage of the main heat exchanger 8, the oxygen-enriched liquid with purity of 80-95% is vaporized and reheated by the main heat exchanger 8 to be discharged out of the cold box, the air liquefying temperature in the system is greatly reduced, the air liquefying temperature and the dew point temperature are further reduced, the lower the corresponding raw material air pressure is, the lower the power consumption of the corresponding air separation device is, and the production cost is reduced.
In some embodiments, the first liquid oxygen can be reheated by the main heat exchanger 8 to be output and stored as an oxygen product, so that byproducts of the whole full-rectification argon-extracting oxygen-enriched air separation process are further enriched.
The upper part of the upper tower 6 is also provided with a dirty nitrogen outlet which is sequentially connected with a dirty nitrogen flow passage of the subcooler 12 and a dirty nitrogen flow passage of the main heat exchanger 8, and is divided into two paths after being vaporized and reheated out of the cold box, the first path is connected with a dirty nitrogen output pipeline, and the first path of dirty nitrogen is discharged in the water cooling tower through the output pipeline; the second path is connected with a purifier polluted nitrogen gas inlet and is used as regeneration gas.
The argon fraction outlet at the lower part of the upper tower 6 is sequentially connected with the argon fraction inlet at the bottom of the first crude argon tower 13, the crude gas argon outlet at the top of the first crude argon tower 13 and the crude gas argon inlet at the bottom of the second crude argon tower 14, namely, the crude gas argon fraction with the argon content of 7-12% is pumped out at the lower part of the upper tower 6 and enters the bottom of the first crude argon tower 13, the crude gas argon fraction rises to the top from the bottom of the first crude argon tower 13 and then enters the bottom of the second crude argon tower 14, and rises to the top from the bottom of the second crude argon tower 14, in the process, the oxygen content in the crude argon fraction is lower and lower, and the process argon with the oxygen content of not more than 1.5PPm is obtained at the top of the second crude argon tower 14.
The first crude argon tower 13 and the second crude argon tower 14 are coupled through a process liquid argon pump 16, and cold sources of the first crude argon tower 13 and the second crude argon tower 14 are from low-pressure liquid air evaporation heat absorption; in theory, the first crude argon column 13 and the second crude argon column 14 should belong to the same equipment, but in the actual production process, the combined height of the first crude argon column 13 and the second crude argon column 14 is too high, which is unfavorable for manufacturing, assembling and construction, so that the first crude argon column 13 and the second crude argon column 14 are separated into two independent crude argon columns, and reflux liquid of the two crude argon columns is sent to the top of the first crude argon column 13 from the bottom of the second crude argon column 14 by using a process liquid argon pump 16, so that the first crude argon column 13 and the second crude argon column 14 are coupled to be similar to one equipment, and the crude argon purification process is realized.
The process argon outlet at the top of the second crude argon tower 14 is divided into two paths, wherein the first path is sequentially connected with the process argon inlet of the crude argon condenser 17 and the crude argon reflux inlet of the second crude argon tower 14, process argon enters the crude argon condenser 17, is condensed by liquid-air heat exchange and then flows back to the second crude argon tower 14 to be used as reflux liquid, and the reflux liquid is pressurized at the bottom of the second crude argon tower 14 by the process liquid argon pump 16 and then is sent to the top of the first crude argon tower 13 to be used as reflux liquid; the second path is connected with a process argon inlet in the middle of the refined argon tower 15, nitrogen is removed in the refined argon tower 15, pure liquid argon with nitrogen content not more than 4PPm is obtained at the bottom of the refined argon tower 15, a cold source at the top of the refined argon tower 15 is evaporated from low-pressure liquid nitrogen, and an evaporation heat source at the bottom of the refined argon tower 15 is condensed from partial gas nitrogen at the top of the lower tower 6.
The pure liquid argon outlet at the bottom of the refined argon tower 15 is connected with a pure liquid argon product conveying pipeline; the gas nitrogen of the refined argon condenser 20 is converged with a dirty nitrogen outlet at the upper part of the upper tower 6 and is connected with a dirty nitrogen runner of the subcooler 12 and the main heat exchanger 8; the crude liquid argon outlet at the bottom of the second crude argon tower 14 is connected with the inlet of a process liquid argon pump 16, is connected with the crude liquid argon inlet at the top of the first crude argon tower 13, and is in reflux connection with the argon fraction at the lower part of the upper tower 6.
According to the full-rectification oxygen-enriched argon extraction process, air flows into the rectification section and the argon extraction section through the air pretreatment section, so that the consumption of electric quantity in the device production and preparation process is greatly reduced compared with an air separation device in the prior art, the variety of products is multiple, the continuous production of enterprises is facilitated, the production cost of the enterprises is reduced, and the economic benefit of the enterprises is improved.
While the invention has been described with reference to preferred embodiments, it is not intended to be limiting. Those skilled in the art will appreciate that various modifications and adaptations can be made without departing from the spirit and scope of the present invention. Accordingly, the scope of the invention is defined by the appended claims.

Claims (7)

1. An oxygen-enriched air separation device for full rectification argon extraction comprises an air pretreatment section, wherein the air pretreatment section is used for preparing dry purified air and transmitting the dry purified air to a rectification section; the device is characterized by further comprising a rectifying section and an argon extracting section;
the rectifying section comprises a lower tower (5), an upper tower (6), a condensing evaporator (7), a main heat exchanger (8), a post-supercharging cooler (9), a supercharger (10), an expander (11), a subcooler (12) and a liquid pump (18); the condensing evaporator (7) is arranged between the lower tower (5) and the upper tower (6);
the argon extracting section comprises a first crude argon tower (13), a second crude argon tower (14), a refined argon tower (15), a process liquid argon pump (16), a crude argon condenser (17), a refined argon evaporator (19) and a refined argon condenser (20);
the air pretreatment section comprises an air filter (1), an air compressor (2), an air cooling tower (3) and a molecular sieve purifier (4) which are connected in sequence; the air pretreatment section is used for drying and impurity-removing raw material air to obtain dry and purified air, and transmitting the dry and purified air to the rectifying section for rectifying and purifying; the air pretreatment section is divided into three paths, wherein the first path is sequentially connected with a first feeding air flow passage of a main heat exchanger (8) and an air inlet at the bottom of a lower tower (5), the second path is sequentially connected with an air inlet of a supercharger (10), an air inlet of a post-supercharging cooler (9), a second feeding air flow passage of the main heat exchanger (8), an air inlet of an expander (11) and an air inlet at the middle part of an upper tower (6), and the third path is connected with an air inlet of an instrument air system;
the nitrogen outlet at the top of the lower tower (5) is divided into two paths, and the first path is connected with the air inlet of the condensation evaporator (7); the second path is connected with an air inlet of a refined argon evaporator (19) at the lower part of the refined argon tower (15);
the oxygen-enriched liquid air outlet at the bottom of the lower tower (5) is connected with the oxygen-enriched liquid air channel of the subcooler (12) and then is divided into two paths, wherein the first path is connected with the oxygen-enriched liquid air inlet at the upper part of the upper tower (6), and the second path is connected with the liquid inlet of the crude argon condenser (17);
the outlet of the liquid nitrogen flow passage of the condensing evaporator (7) is divided into two paths, the first path is connected with a liquid nitrogen reflux port at the top of the lower tower (5), and the second path is connected with a liquid nitrogen flow passage of the subcooler (12);
the liquid nitrogen runner outlet of the subcooler (12) is divided into three paths, the first path is connected with a liquid nitrogen reflux port at the top of the upper tower (6), the second path is used as product liquid nitrogen to be connected with a pure liquid nitrogen product conveying pipeline, and the third path is connected with a liquid nitrogen inlet of the refined argon condenser (20);
the bottom of the upper tower (6) is connected with the condensation evaporator (7), liquid oxygen at the bottom of the upper tower (6) enters the condensation evaporator (7), the liquid oxygen is divided into two paths from the outlet of the condensation evaporator (7), the first path is used as product liquid oxygen to be connected with a pure liquid oxygen product conveying pipeline, the second path is sequentially connected with a liquid pump (18) and an oxygen-enriched liquid air outlet at the bottom of the lower tower (5), and the converged liquid is connected with a liquid oxygen evaporation runner of the main heat exchanger (8);
the dirty nitrogen outlet at the upper part of the upper tower (6) is connected with a subcooler (12) and a dirty nitrogen flow passage of the main heat exchanger (8);
the pure nitrogen outlet at the top of the upper tower (6) is connected with a pure nitrogen runner of the subcooler (12) and the main heat exchanger (8);
an argon fraction outlet at the lower part of the upper tower (6) is sequentially connected with an argon fraction inlet at the bottom of the first crude argon tower (13), a crude gas argon outlet at the top of the first crude argon tower (13) and a crude gas argon inlet at the bottom of the second crude argon tower (14);
the process argon outlet at the top of the second crude argon tower (14) is divided into two paths, the first path is connected with a process argon inlet of a crude argon condenser (17) and a crude argon reflux port of the second crude argon tower (14) in sequence, and the second path is connected with a process argon inlet at the middle part of the refined argon tower (15);
a pure liquid argon outlet at the bottom of the refined argon tower (15) is connected with a pure liquid argon product conveying pipeline;
the gas nitrogen of the refined argon condenser (20) is converged with a dirty nitrogen outlet at the upper part of the upper tower (6) and is connected with a dirty nitrogen runner of the subcooler (12) and the main heat exchanger (8);
the crude liquid argon outlet at the bottom of the second crude argon tower (14) is connected with the inlet of a process liquid argon pump (16), is connected with the crude liquid argon inlet at the top of the first crude argon tower (13), and is in reflux connection with the argon fraction at the lower part of the upper tower (6);
the rectifying section also comprises a liquid nitrogen production line; the liquid nitrogen production line is from an air pretreatment section dry air outlet to a condensing evaporator (7) liquid nitrogen outlet through a first feeding air flow passage of a main heat exchanger (8), an air inlet at the bottom of a lower tower (5), a nitrogen outlet at the top of the lower tower (5) and a nitrogen inlet of the condensing evaporator (7).
2. The full-rectification argon-extracting oxygen-enriched air separation device according to claim 1, wherein a liquid nitrogen outlet of the liquid nitrogen production line is divided into four paths, the first path is sequentially connected with a liquid nitrogen runner of a subcooler (12) and a liquid nitrogen inlet of an upper tower (6), the second path is connected with a liquid inlet of a refined argon condenser (20) at the upper part of a refined argon tower (15), the third path is connected with a liquid nitrogen reflux port of a lower tower (5), and the fourth path is connected with a liquid nitrogen product output pipeline.
3. The full-rectification argon-oxygen-enriched air separation device according to claim 1, wherein the rectification section comprises a gas nitrogen production line;
the first path of the air nitrogen production line passes through a first feeding air flow passage of the main heat exchanger (8), a bottom air inlet of the lower tower (5), a middle liquid air inlet of the upper tower (6), a top liquid nitrogen inlet of the upper tower (6) and a top nitrogen outlet of the upper tower (6) from a dry air outlet of the air pretreatment section; the second path is through booster compressor (10) air inlet, booster aftercooler (9) air inlet, main heat exchanger (8) second feeding air runner, expander (11) air inlet, upper tower (6) middle part air inlet to upper tower (6) top nitrogen gas export.
4. The full-rectification argon-extracting oxygen-enriched air separation device according to claim 3, wherein a nitrogen outlet of the gas nitrogen production line is directly connected with a nitrogen product output pipeline.
5. The full-rectification argon-extracting oxygen-enriched air separation device according to claim 1, wherein the first crude argon column (13) and the second crude argon column (14) are coupled by a process liquid argon pump (16).
6. The full-rectification argon-extracting oxygen-enriched air separation device according to claim 2, wherein a first throttle valve is arranged between a liquid nitrogen flow passage of a first path of liquid nitrogen outlet of the condensing evaporator (7) and a liquid nitrogen inlet of the upper tower (6); a second throttle valve is arranged between a liquid nitrogen outlet second path of the condensation evaporator (7) and a liquid inlet of a refined argon condenser (20) at the upper part of the refined argon tower (15); a third throttle valve is arranged between an oxygen-enriched liquid air channel of the first outlet of the oxygen-enriched liquid air at the bottom of the lower tower (5) and an oxygen-enriched liquid air inlet at the upper part of the upper tower (6); a fourth throttle valve is arranged between an oxygen-enriched liquid air flow passage of the oxygen-enriched liquid air outlet at the bottom of the lower tower (5) and a liquid inlet of the crude argon condenser (17).
7. A full-rectification argon-extracting oxygen-enriched air separation process, which is characterized by adopting the air separation device as claimed in claim 1, comprising the following steps:
1) Raw material air is filtered, compressed, cooled and purified to obtain dry purified air, the dry purified air is divided into three paths, the first path enters a main heat exchanger (8), exchanges heat with reflux gas, is cooled to a liquefaction temperature, and enters a lower tower (5) to participate in rectification; the second path of dry purified air enters a main heat exchanger (8) to exchange heat with the reflux gas to the temperature before expansion after being pressurized and cooled, then enters an expander (11) to refrigerate, and enters an upper tower (6) to participate in rectification; the third path of dry purified air is conveyed to an instrument air system to serve as instrument air and sealing air;
2) In the rectifying section, air and reflux liquid nitrogen in a lower tower (5) are repeatedly condensed and evaporated on a plurality of layers of tower plates, oxygen-enriched liquid air is accumulated at the bottom of the lower tower (5), the oxygen-enriched liquid air is supercooled by a supercooler (12) and then is divided into two paths, one path of the oxygen-enriched liquid air enters the upper part of an upper tower (6) to be used as a raw material of the upper tower (6), the other path of the oxygen-enriched liquid air enters a crude argon condenser (17) to be used as a top cold source of a first crude argon tower (13) and a second crude argon tower (14) after being throttled, and steam enters the upper tower (6) as a raw material; the nitrogen at the top of the lower tower (5) is condensed into liquid nitrogen by a condensing evaporator (7) and then divided into four paths, and the first path of liquid nitrogen is supercooled by a supercooler (12), throttled and decompressed and then sprayed into the top of the upper tower (6) to be used as reflux liquid of the upper tower (6); the second liquid nitrogen enters a refined argon condenser (20) in a throttling way to be used as a top cold source of a refined argon tower (15); the third liquid nitrogen is taken as a product to enter a storage tank; the fourth liquid nitrogen returns to the lower tower (5) as reflux liquid; a small amount of gas nitrogen at the top of the lower tower enters a refined argon evaporator to be used as a bottom heat source of a refined argon tower (15);
3) Pure nitrogen is obtained at the top of the upper tower (6), and enters a main heat exchanger (8) for reheating to obtain nitrogen product after being supercooled by a cooler (12); the upper part of the upper tower (6) is provided with dirty nitrogen, the dirty nitrogen is supercooled by a supercooler (12) and is reheated by a main heat exchanger (8) to be discharged out of the cold box, a part of the depurating device is used as regenerated gas, and the rest of the dewatering cold tower is emptied; the liquid oxygen of the product at the bottom of the upper tower (6) enters a main condensing evaporator (7) for evaporation, the evaporated oxygen is used as rising steam of the upper tower (6), part of the liquid oxygen is pressurized by a low-temperature liquid pump (18) and then is converged with the oxygen-enriched liquid air at the bottom of the lower tower, and is vaporized and re-heated by a main heat exchanger (8) to be discharged out of a cold box, and part of the liquid oxygen is used as the product to enter a storage tank;
4) The crude gas argon fraction extracted from the bottom of the upper tower (6) enters the bottom of a first crude argon tower (13), rises from the bottom of the first crude argon tower (13) to the top, then enters the bottom of a second crude argon tower (14), rises from the bottom of the second crude argon tower (14) to the top, and in the process, the oxygen content in the crude liquid argon fraction is lower and lower, and process argon is obtained from the top of the second crude argon tower (14); the process argon is divided into two paths from the top of the second crude argon tower (14) through a conveying pipeline, one path enters a crude argon condenser (17), and is condensed with liquid-air heat exchange and then flows back to the second crude argon tower (14) to serve as reflux liquid, and the reflux liquid is fed to the bottom of the second crude argon tower (14) to serve as reflux liquid after being pressurized by a process liquid argon pump (16); the other path of process argon is sent to the middle part of the refined argon tower (15), nitrogen is removed in the refined argon tower (15), and pure liquid argon is obtained at the bottom of the refined argon tower (15).
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