CN108759311B - Air separation device and method for preparing large liquid volume - Google Patents

Air separation device and method for preparing large liquid volume Download PDF

Info

Publication number
CN108759311B
CN108759311B CN201810765000.9A CN201810765000A CN108759311B CN 108759311 B CN108759311 B CN 108759311B CN 201810765000 A CN201810765000 A CN 201810765000A CN 108759311 B CN108759311 B CN 108759311B
Authority
CN
China
Prior art keywords
pipeline
tower
liquid
air
argon
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Active
Application number
CN201810765000.9A
Other languages
Chinese (zh)
Other versions
CN108759311A (en
Inventor
骞绍显
卓跃光
王庆波
韦向攀
彭喜魁
刘洪仁
陈洪杰
张伟杰
王志锋
杨文娟
苏建龙
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Kaifeng Air Separation Group Co ltd
Original Assignee
Kaifeng Air Separation Group Co ltd
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Kaifeng Air Separation Group Co ltd filed Critical Kaifeng Air Separation Group Co ltd
Priority to CN201810765000.9A priority Critical patent/CN108759311B/en
Publication of CN108759311A publication Critical patent/CN108759311A/en
Application granted granted Critical
Publication of CN108759311B publication Critical patent/CN108759311B/en
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04036—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of 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
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04042—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of argon or argon enriched stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/042—Division of the main heat exchange line in consecutive sections having different functions having an intermediate feed connection
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or 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
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
    • 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
    • F25J3/04642—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
    • 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

Landscapes

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

Abstract

The invention relates to an air separation device and method for preparing large liquid amount, wherein the device comprises an air filter, an air compressor, a purification unit, a supercharger, a high-low temperature supercharging turbine expander and a cryogenic separation cold box unit. The method for preparing the air separation device with large liquid quantity by cryogenic separation disclosed by the invention adopts the pressurized air middle pumping, the double-pressurizing double-expansion of the high-low temperature pressurizing turbine expander enters the lower tower, the product oxygen and nitrogen uses the double-pump compression flow and the total reflux form of the argon preparation system, thereby meeting the requirements of large liquid quantity air separation and large cold quantity, fully utilizing the circulation of material flows, reducing equipment, reducing energy consumption and improving extraction rate.

Description

Air separation device and method for preparing large liquid volume
Technical Field
The invention relates to the technical field of air low-temperature separation, in particular to an air separation device and method for preparing large liquid volume.
Background
With the rapid development of the steel and chemical industry, the demand for industrial gases such as oxygen, nitrogen and argon has also increased greatly, and in particular, the demand for gaseous and liquid products has increased together for the same user in different production stages. The gaseous product has the advantages of convenient supply, quick utilization and the like, and the liquid product has the advantages of convenient storage and transportation and the like. The conventional external compression air separation unit can produce 10% liquid product at most, and the conventional internal compression air separation unit can produce 20% liquid product at most. In recent two years, the requirements of government ecological environment protection are imposed, the production characteristics of some enterprises are forced to change, and the requirements of space devices are changed accordingly, so that the requirements of normal gas products are met, and the production of large quantities of liquid is considered. In recent years, a plurality of gas companies are used for intensively supplying gas in chemical industry parks with higher centralization degree, the gas companies are used for producing and supplying gas during normal production of enterprises, and the gas companies are used for producing a large amount of liquid products and then are transported out of the tank wagon for sale during reduction production of the enterprises. The conventional gas air separation device and the conventional full-liquid air separation device obviously cannot meet the production requirements of enterprises and gas companies, so that the energy consumption of the device is increased, and the energy conservation, the emission reduction and the ecological environment protection are not facilitated. In this situation, the development of an air separation unit for producing a large amount of liquid has been a trend. The air separation device not only meets the requirements of conventional gas products, but also can prepare about 50% of liquid products at the same time, integrates the advantages of the conventional gas air separation device and the conventional full-liquid air separation device, simultaneously meets different requirements of users, improves the unbalanced supply and demand of gas and liquid, and brings higher economic benefit to the sales of liquid products.
The core of the air low-temperature separation method is that the difference of boiling points of all components in the air is utilized to realize the separation of a gas mixture in a rectifying tower, the basic principle is that an expander is utilized to carry out adiabatic expansion refrigeration and Joule-Thomson throttling refrigeration effect, process air with certain pressure is expanded and throttled to generate lower temperature, and the components in the air can be separated to obtain gas and liquid products by heat exchange and cold recovery. The cooling capacity of the whole system is mostly ensured by the adiabatic expansion of the expander. To prevent solidification of impurity components in air at low temperature to block heat exchanger and pipesThus, the separation of air by low temperature requires pretreatment of the air before entering the cold box to remove components such as CO which are solidified at low temperature 2 And H 2 O。
The air separation plant is mainly consumed by the air, and the main consumption is electric energy, and is particularly critical to the energy consumption of the air separation plant with large liquid quantity, so that how to further reduce the energy consumption is particularly important in the air separation plant. For air separation plants employing cryogenic rectification, energy consumption and extraction rate are also the main parameters for evaluating plant economic and technical metrics. For the users who need the air separation device of gas and large liquid volume simultaneously, reduce the energy consumption of device and improve the extraction rate, can effectively satisfy the reduction in production cost when production needs, be favorable to energy saving and emission reduction and ecological environment protection.
At present, the internal compression space diversion process mainly comprises a low-pressure expansion upper tower feeding process and a medium-pressure expansion lower tower feeding process. The liquid amount prepared by low-pressure expansion into the upper tower is small, and the requirement of large liquid amount can not be met at all; the liquid amount produced by the medium-pressure expansion into the lower tower process is about 20%, and if a large amount of liquid is produced, a large amount of air is required to be increased, so that the energy consumption of the device is increased.
Disclosure of Invention
The invention aims to overcome the defects in the prior art and provide a space separation device and a method for preparing a gas product and simultaneously preparing a large amount of liquid by double expansion of a high-temperature expander and a low-temperature expander, thereby reducing the operation cost and the energy consumption of the device.
The technical scheme of the invention is realized as follows: the air separation device comprises an air filter, an air compressor, an air purification unit, an air booster, a low-temperature machine pressurizing end, a low-temperature expansion machine expansion end, a low-temperature machine pressurizing end cooler, a high-temperature machine pressurizing end, a high-temperature expansion machine expansion end, a high-temperature machine pressurizing end cooler and a cryogenic separation cold box unit, wherein the cryogenic separation cold box unit comprises a main heat exchanger, a lower tower, a condensing evaporator, an upper tower, a subcooler, a liquid nitrogen pump, a liquid oxygen pump, a crude argon tower I, a crude argon tower II, a circulating liquid argon pump, a refined argon tower and a throttle valve, the crude argon tower I comprises a tower body and a condenser at the top of the tower body, the refined argon tower comprises a tower body, a condenser at the top of the tower body and an evaporator at the bottom of the tower body, a raw material atmosphere is input into an inlet of the air compressor through the air filter, and an outlet of the air compressor is communicated with an inlet of the air purification unit through a first pipeline, the air purification unit outlet is respectively communicated with a second pipeline and a third pipeline, the second pipeline is communicated with the bottom inlet of the lower tower through a main heat exchanger, the third pipeline is communicated with the inlet of the air booster, the air booster outlet is communicated with the bottom inlet of the lower tower through a fourth pipeline through a main heat exchanger and a fifth throttle valve, the bottom outlet of the lower tower is communicated with the condenser inlet of the crude argon tower I through an eleventh pipeline through a cooler, a refined argon tower evaporator and a first throttle valve, the bottom outlet of the lower tower is respectively communicated with a twelfth pipeline and a thirteenth pipeline through a cooler, the twelfth pipeline is communicated with the middle inlet of the upper tower through a second throttle valve, the thirteenth pipeline is communicated with the condenser inlet of the refined argon tower through a third throttle valve, the outlet at the top of the lower tower is communicated with the inlet of the condensing evaporator through a fourteenth pipeline, the outlet at the lower part of the condensing evaporator is connected with a fifteenth pipeline, the fifteenth pipeline is respectively communicated with a sixteenth pipeline, a seventeenth pipeline and an eighteenth pipeline, the sixteenth pipeline is communicated with the inlet at the top of the lower tower, the seventeenth pipeline is communicated with the cryogenic separation cold box unit through a liquid nitrogen pump and a main heat exchanger, the eighteenth pipeline is respectively communicated with a nineteenth pipeline and a twentieth pipeline through a supercooler, the nineteenth pipeline is communicated with the inlet at the upper part of the upper tower through a fourth throttle valve, the twentieth pipeline is communicated with the cryogenic separation cold box unit, the outlet at the bottom of the condensing evaporator is respectively communicated with a twenty first pipeline and a twenty second pipeline, the twenty first pipeline is communicated with the cryogenic separation cold box unit through a liquid oxygen pump and the main heat exchanger, the twenty-second pipeline is out of the cryogenic separation cold box unit, the outlet of the top of the upper tower is communicated with a twenty-third pipeline, the twenty-third pipeline is communicated with the air purification unit through a subcooler and a main heat exchanger, the bottom of the upper tower is connected with a twenty-fourth pipeline, the twenty-fourth pipeline is in butt joint with the twenty-third pipeline, the outlet of the middle lower part of the upper tower is communicated with the inlet of the bottom of the crude argon tower II through a thirty-first pipeline, the top of the crude argon tower II is communicated with the bottom of the crude argon tower I through a thirty-second pipeline, the bottom of the crude argon tower I is communicated with the upper part of the crude argon tower II through a circulating liquid argon pump through a thirty-third pipeline, the bottom of the crude argon tower II is communicated with the inlet of the middle lower part of the upper tower through a thirty-fourth pipeline, the outlet of the crude argon tower I is respectively communicated with the thirty-fifth pipeline and the thirty-sixth pipeline, the thirty-fifth pipeline is communicated with the upper part of the crude argon tower I, the thirty-sixth pipeline is communicated with the middle part of the refined argon tower, the top of the crude argon tower I condenser is communicated with the inlet of the middle part of the upper tower through a thirty-seventh pipeline, the upper part of the refined argon tower condenser is connected with a thirty-eighth pipeline, the thirty-eighth pipeline is in butt joint with the thirty-seventh pipeline, the top of the refined argon tower condenser is connected with a thirty-ninth pipeline, the thirty-ninth pipeline is out of the cryogenic separation cold box unit, the bottom of the refined argon tower evaporator is connected with a fortieth pipeline, and the fortieth pipeline is out of the cryogenic separation cold box unit.
The lower tower is a sieve plate tower or a structured packing tower, and the upper tower, the crude argon tower I, the crude argon tower II and the refined argon tower are structured packing towers. The main heat exchanger, the condensing evaporator, the subcooler, the crude argon tower I condenser, the refined argon tower evaporator and the condenser are all vacuum brazing plate-fin heat exchangers.
The air booster is provided with a middle extraction opening, the middle extraction opening is respectively communicated with a fifth pipeline and a sixth pipeline, the fifth pipeline is sequentially communicated with the inlet at the bottom of the lower tower through the low-temperature booster end, the low-temperature booster end cooler, the high-temperature booster end cooler, the main heat exchanger and the expansion end of the low-temperature expander, and the sixth pipeline is sequentially communicated with the inlet at the bottom of the lower tower through the main heat exchanger and the expansion end of the high-temperature expander, and the main heat exchanger is communicated with the inlet at the bottom of the lower tower.
The bottom of the crude argon tower I condenser is provided with a liquid-air reflux port, the liquid-air reflux port is connected with a forty-first pipeline, the forty-first pipeline is communicated with an inlet at the middle part of the upper tower, the upper part of the crude argon tower I condenser is provided with a liquid-air overflow port, the liquid-air overflow port is connected with a forty-second pipeline, and the forty-second pipeline is communicated with the forty-first pipeline.
A method for preparing a large amount of liquid by using the device, which comprises the following steps:
1) The raw material air is filtered by an air filter to remove impurities, then enters an air compressor for compression, and then enters an air purification unit through a first pipeline to remove CO 2 、H 2 O and part of hydrocarbon are divided into two parts: one part enters the main heat exchanger through the second pipeline to be cooled to a certain temperature, and then enters the bottom of the lower tower to participate in rectification after exiting the main heat exchanger; the other part enters an air booster through a third pipeline to be boosted, is pumped out from a final stage, enters a main heat exchanger through a fourth pipeline to be cooled into liquid air, and enters the middle lower part of a lower tower to participate in rectification after being throttled by a throttle valve.
2) Obtaining nitrogen at the top of the tower after preliminary rectification by a lower tower, obtaining lean liquid space at the middle lower part of the lower tower, and obtaining oxygen-enriched liquid space at the bottom of the lower tower; the nitrogen at the top of the lower tower enters a condensing evaporator through a fourteenth pipeline to be condensed into liquid nitrogen, one part of the liquid nitrogen returns to the lower tower through a sixteenth pipeline to be used as reflux liquid, the other part of the liquid nitrogen enters a main heat exchanger to be reheated to normal temperature after being pressurized to a required pressure through a liquid nitrogen pump to be used as a nitrogen product to go out of a cryogenic separation cold box, the other part of the liquid nitrogen enters a subcooler through an eighteenth pipeline to be subcooled, and the other part of the liquid nitrogen enters the upper tower to be used as reflux liquid of the upper tower after being throttled through a nineteenth pipeline to participate in rectification, and the other part of the liquid nitrogen enters the twenty-first pipeline to be used as a liquid nitrogen product to go out of the cryogenic separation cold box; the lean liquid air at the middle lower part of the lower tower is divided into two parts after being supercooled by a subcooler, one part enters the middle upper part of the upper tower to participate in rectification after being throttled by a twelfth pipeline, and the other part enters the refined argon tower condenser to serve as a cold source after being throttled by a thirteenth pipeline; the oxygen-enriched liquid air at the bottom of the lower tower enters an evaporator of the refined argon tower through an eleventh pipeline to serve as a heat source; part of liquid oxygen from the upper tower is evaporated into oxygen in a condensation evaporator to be used as ascending gas of the upper tower to participate in rectification, part of the oxygen is pressurized to the required pressure by a liquid oxygen pump through a twenty-first pipeline and then enters a main heat exchanger to be reheated to normal temperature to be used as an oxygen product to be discharged into a cryogenic separation cold box, and part of the oxygen is used as the liquid oxygen product to be discharged into the cryogenic separation cold box through a twenty-second pipeline; low-pressure nitrogen is obtained at the top of the upper tower, the low-pressure nitrogen is reheated by the subcooler and the main heat exchanger, then the low-pressure nitrogen is removed from the air purification unit to be recycled, and then the recycled air is exhausted, a small part of oxygen is extracted from the bottom of the upper tower to be used as a means for adjusting the argon content of the argon fraction, and the extracted oxygen is converged into a twenty-third pipeline after passing through the subcooler through a twenty-fourth pipeline.
3) A certain amount of argon fraction is pumped from the middle lower part of the upper tower and enters the bottom of a crude argon tower II through a thirty-first pipeline, the argon fraction is rectified and pumped from the top and enters the bottom of the crude argon tower I through a thirty-second pipeline, liquid argon at the bottom of the crude argon tower I is pressurized through a circulating liquid argon pump and then is sent to the upper part of the crude argon tower II to be used as reflux liquid to participate in rectification, liquid at the bottom of the crude argon tower II is returned to an upper tower argon fraction pumping position through a thirty-fourth pipeline to participate in rectification, a condenser cold source of the crude argon tower I adopts oxygen-enriched liquid air from the bottom of a lower tower kettle after being throttled through an eleventh pipeline, a process argon part from the upper part of the crude argon tower I is condensed, and the oxygen-enriched liquid air part is evaporated; the liquid argon at the bottom of the condenser of the crude argon column I flows back to the crude argon column I through a thirty-fifth pipeline to be used as reflux liquid to participate in rectification, the process argon is sent to the middle part of the refined argon column through a thirty-sixth pipeline to participate in rectification, and the liquid air steam at the top of the condenser of the crude argon column I returns to the upper column through a thirty-seventh pipeline; the lean liquid air throttled by the third throttle valve through the thirteenth pipeline is adopted as the cold source of the condenser of the refined argon tower, the lean liquid air is evaporated into liquid air steam which is converged with the liquid air steam of the thirty-seventh pipeline through the thirty-eighth pipeline, partial process argon is discharged from the top of the condenser of the refined argon tower through the thirty-ninth pipeline, the heat source of the evaporator of the refined argon tower adopts the oxygen-enriched liquid air of the lower tower kettle through the eleventh pipeline, and pure liquid argon in the evaporator of the refined argon tower is discharged from the cryogenic separation cold box through the fortieth pipeline.
The air booster is provided with a middle extraction port, 2.8MPa and 40 ℃ air extracted from the middle extraction port is divided into two streams, one stream of middle extraction air sequentially passes through the pressurization of the pressurization end of the low-temperature machine, the cooling of the pressurization end cooler of the low-temperature machine, the pressurization of the pressurization end cooler of the high-temperature machine and the cooling of the pressurization end cooler of the high-temperature machine through a fifth pipeline, enters the main heat exchanger to be cooled to minus 95 ℃ in the state of the temperature of 40 ℃ and the pressure of 6.0MPa, is extracted, enters the expansion end of the low-temperature machine to be expanded to the pressure of 0.48MPa and the temperature of minus 173 ℃ to enter the bottom of the lower tower to participate in rectification, and the other stream of air enters the main heat exchanger to be cooled to 5 ℃ through a sixth pipeline, is extracted from the middle of the main heat exchanger to enter the expansion end of the high-temperature machine to be expanded to the pressure of 0.48MPa and the temperature of minus 84 ℃ and then returns to the main heat exchanger to be cooled to minus 167 ℃ to enter the bottom of the lower tower to participate in rectification.
The bottom of the condenser of the crude argon tower I is provided with a liquid-air reflux port, most liquid air flows back to the middle part of the upper tower through a forty-first pipeline to participate in rectification, the upper part of the condenser of the crude argon tower I is provided with a liquid-air overflow port, and part of liquid air overflows into the forty-first pipeline through a forty-second pipeline.
The technical scheme of the invention has the following beneficial effects:
the refrigerating system of the device adopts two specifications of a low-temperature booster turbo-expander and a high-temperature booster turbo-expander, the arrangement sequence of the booster ends 5 of the low-temperature machines is in front, the booster ends 7 of the high-temperature machines are in back, the stable operation of the expander is facilitated, and the expansion work of the turbo-expander is fully utilized to boost the medium-pressure air again; the expansion end 10 of the high-temperature expansion machine adopts normal-temperature medium-pressure air cooled by the main heat exchanger 11, and the expansion end 9 of the low-temperature expansion machine adopts high-pressure air which is pressurized by the pressurization end 5 of the low-temperature machine and the pressurization end 7 of the high-temperature machine and cooled to low temperature by the main heat exchanger 11. The high-low temperature expansion machine adopts expansion media with different qualities, fully exerts the refrigeration effect, and well meets the cold energy required by the large-liquid-quantity air separation device.
The device crude argon column I19 condenser adopts total reflux, namely the lower tower bottom oxygen-enriched liquid air is supercooled and then enters the refined argon column 21 evaporator to be used as a heat source, and then enters the crude argon column I19 condenser to be used as a cold source after being throttled by the first throttle valve 22, and then flows back to the middle part of the upper column 14 to participate in rectification, thereby fully utilizing the potential energy of the oxygen-enriched liquid air, changing the traditional method of adopting the lower tower pressure nitrogen as the heat source of the refined argon column evaporator, saving the processing air quantity and saving the energy consumption.
The lower tower 12 adopts a high-efficiency convection double overflow sieve plate tower, so that the rectification efficiency is high; the upper tower 14 and the argon tower adopt packed towers, so that the rectification effect is good, the operation elasticity is high, the method is suitable for variable working condition operation, and the method can adapt to the working condition of relatively large gas-liquid ratio.
Drawings
FIG. 1 is a schematic diagram showing the connection structure of an air separation apparatus and method for preparing a large amount of liquid according to the present invention.
1. An air filter, 2, an air compressor, 3, an air purification unit, 4, an air booster, 5, a low-temperature booster end, 6, a low-temperature booster end cooler, 7, a high-temperature booster end, 8, a high-temperature booster end cooler, 9, a low-temperature expander expansion end, 10, a high-temperature expander expansion end, 11, a main heat exchanger, 12, a lower column, 13, a condensation evaporator, 14, an upper column, 15, a subcooler, 16, a liquid nitrogen pump, 17, a liquid oxygen pump, 18, a crude argon column I, 19, a crude argon column II, 20, a circulating liquid argon pump, 21, a refined argon column, 22, a first throttle valve, 23, a second throttle valve, 24, a third throttle valve, 25, a fourth throttle valve, 26, a fifth throttle valve, 27, a cryogenic separation cold box unit, 101, a first pipeline, 102, a second pipeline, 103, a third pipeline, 104, fourth pipe, 105, fifth pipe, 106, sixth pipe, 111, eleventh pipe, 112, twelfth pipe, 113, thirteenth pipe, 114, fourteenth pipe, 115, fifteenth pipe, 116, sixteenth pipe, 117, seventeenth pipe, 118, eighteenth pipe, 119, nineteenth pipe, 120, twentieth pipe, 121, twenty first pipe, 122, twenty second pipe, 123, twenty third pipe, 124, twenty fourth pipe, 131, thirty first pipe, 132, thirty second pipe, 133, thirty third pipe, 134, thirty fourth pipe, 135, thirty fifth pipe, 137, thirty seventh pipe, 138, thirty eighth pipe, 139, thirty ninth pipe, 140, fortieth pipe, 141, fortieth pipe, 142, fortieth pipe.
Detailed Description
The invention is further illustrated and described below in conjunction with the specific embodiments and the accompanying drawings.
As shown in figure 1, the air separation device for preparing large liquid volume comprises an air filter 1, an air compressor 2, an air purification unit 3, an air booster 4, a low-temperature machine booster end 5, a low-temperature expansion machine expansion end 9, a low-temperature machine booster end cooler 6, a high-temperature machine booster end 7, a high-temperature expansion machine expansion end 10, a high-temperature machine booster end cooler 8 and a cryogenic separation cold box unit 27, wherein the cryogenic separation cold box unit 27 comprises a main heat exchanger 11, a lower tower 12, a condensation evaporator 13, an upper tower 14, a subcooler 15, a liquid oxygen pump 16, a liquid oxygen pump 17, a crude argon tower I18, a crude argon tower II 19, a circulating liquid argon pump 20, a refined argon tower 21, a first throttle valve 22, a second throttle valve 23, a third throttle valve 24, a fourth throttle valve 25 and a fifth throttle valve 26, the crude argon tower I18 comprises a tower body and a condenser at the top of the tower body, the refined argon tower 21 comprises a tower body, a condenser at the top of the tower body and an evaporator at the bottom of the tower body, wherein the inlet of the air compressor 2 is input into the raw material atmosphere through an air filter 1, the outlet of the air compressor 2 is communicated with the inlet of the air purification unit 3 through a first pipeline 101, the outlet of the air purification unit 3 is respectively communicated with a second pipeline 102 and a third pipeline 103, the second pipeline 102 is communicated with the inlet at the bottom of the lower tower 12 through the main heat exchanger 11, the third pipeline 103 is communicated with the inlet of the air booster 4, the outlet of the air booster 4 is communicated with the inlet at the middle and lower parts of the lower tower 12 through the main heat exchanger 11 and a fifth throttle valve 26 through a fourth pipeline 104, the outlet at the bottom of the lower tower 12 is communicated with the inlet of the condenser of the crude argon tower I18 through an eleventh pipeline 111 and the evaporator of the refined argon tower 21 and the first throttle valve 22, the outlet at the middle and lower parts of the lower tower 12 is respectively communicated with a twelfth pipeline 112 and a thirteenth pipeline 113 through a subcooler 15, the twelfth pipeline 112 is communicated with the inlet at the middle part of the upper tower 14 through a second throttle valve 23, the thirteenth pipeline 113 is communicated with the condenser inlet of the refined argon tower 21 through a third throttle valve 24, the outlet at the top of the lower tower 12 is communicated with the inlet of the condensation evaporator 13 through a fourteenth pipeline 114, the outlet at the lower part of the condensation evaporator 13 is connected with a fifteenth pipeline 115, the fifteenth pipeline 115 is respectively communicated with a sixteenth pipeline 116, a seventeenth pipeline 117 and an eighteenth pipeline 118, the sixteenth pipeline 116 is communicated with the inlet at the top of the lower tower 12, the seventeenth pipeline 117 is discharged from the cryogenic separation cold box unit 27 through a liquid nitrogen pump 16 and a main heat exchanger 11, the eighteenth pipeline 118 is respectively communicated with a nineteenth pipeline 119 and a twentieth pipeline 120 through the subcooler 15, the nineteenth pipeline 119 is communicated with the upper inlet of the upper tower 14 through a fourth throttle valve 25, the twentieth pipeline 120 is communicated with the cryogenic separation cold box unit 27, the bottom outlet of the condensation evaporator 13 is respectively communicated with a twenty-first pipeline 121 and a twenty-second pipeline 122, the twenty-first pipeline 121 is communicated with the cryogenic separation cold box unit 27 through a liquid oxygen pump 17 and a main heat exchanger 11, the twenty-second pipeline 122 is communicated with the cryogenic separation cold box unit 27, the top outlet of the upper tower 14 is communicated with a twenty-third pipeline 123, the twenty-third pipeline 123 is communicated with the air purification unit 3 through a subcooler 15 and a main heat exchanger 11, the bottom of the upper tower 14 is connected with a twenty-fourth pipeline 124, the twenty-fourth pipeline 124 is in butt joint with the twenty-third pipeline 123, the bottom outlet of the upper tower 14 is communicated with the bottom inlet of the crude argon tower II 19 through a thirty-first pipeline 131, the top of the crude argon tower II 19 is communicated with the bottom of the crude argon tower I18 through a thirty-second pipeline 132, the bottom of the crude argon tower I18 is communicated with the upper part of the crude argon tower II 19 through a thirty-third pipeline 133 through a circulating liquid argon pump 20, the bottom of the crude argon tower II 19 is communicated with the bottom inlet of the upper tower 14 through a thirty-fourth pipeline 134, the condenser outlet of the crude argon tower I18 is respectively communicated with a thirty-fifth pipeline 135 and a thirty-sixth pipeline 136, the thirty-fifth pipeline 135 is communicated with the upper part of the crude argon tower I18, the thirty-sixth pipeline 136 is communicated with the middle part of the refined argon tower 21, the top of the crude argon tower I18 is communicated with the middle inlet of the upper tower 14 through a thirty-seventh pipeline 137, the upper part of the refined tower 21 is connected with an eighth argon pipeline 138, the thirty-eighth pipeline 138 is respectively communicated with the thirty-eighth pipeline 135 and the thirty-eighth pipeline 137, the thirty-eighth pipeline 137 is connected with the fortieth pipeline 21, the thirty-third pipeline 21 is connected with the thirty-third pipeline 27, the thirty-third pipeline 33 is connected with the cool unit and the thirty-third pipeline 139, and the thirty-third pipeline is connected with the top unit 139.
The lower column 12 is a sieve tray column or a structured packing column, and the upper column 14, the crude argon columns I18, II 19, and the refined argon column 21 are structured packing columns. The main heat exchanger 11, the condensing evaporator 13, the subcooler 15, the condenser of the crude argon column I18, the evaporator of the refined argon column 21 and the condenser are all vacuum brazing plate-fin heat exchangers.
The air booster 4 is provided with a middle extraction port, the middle extraction port is respectively communicated with a fifth pipeline 105 and a sixth pipeline 106, the fifth pipeline 105 is sequentially communicated with the bottom inlet of the lower tower 12 through the low-temperature booster end 5, the low-temperature booster end cooler 6, the high-temperature booster end 7, the high-temperature booster end cooler 8, the main heat exchanger 11 and the low-temperature expander expansion end 9, and the sixth pipeline 106 is sequentially communicated with the bottom inlet of the lower tower 12 through the main heat exchanger 11 and the high-temperature expander expansion end 10, and the main heat exchanger 11 is sequentially communicated with the bottom inlet of the lower tower 12.
The bottom of the crude argon column I18 condenser is provided with a liquid-air reflux port, the liquid-air reflux port is connected with a forty-first pipeline 141, the forty-first pipeline 141 is communicated with an inlet in the middle of the upper column 14, the upper part of the crude argon column I18 condenser is provided with a liquid-air overflow port, the liquid-air overflow port is connected with a forty-second pipeline 142, and the forty-second pipeline 142 is communicated with the forty-first pipeline 141.
The method for utilizing the large-liquid-volume air separation device comprises the following steps:
1) The raw material of the device is air, the air is filtered by an air filter 1, enters an air compressor 2 for compression, the air pressure after compression is 0.5MPa, and then enters an air purification unit 3 through a first pipeline 101 for removing CO 2 、H 2 O and part of hydrocarbon are divided into two parts, one part enters the main heat exchanger 11 through the second pipeline 102 to be cooled to about-167 ℃, and then enters the bottom of the lower tower 12 to participate in rectification after exiting the main heat exchanger 11; the other part enters an air booster 4 through a third pipeline 103 for boosting, enters a liquid space cooled to about-167 ℃ through a fourth pipeline 104 after the final stage of the air booster is boosted to 6.0MPa, enters a main heat exchanger 11 for cooling, and enters the middle lower part of a lower tower 12 through a fifth throttle valve 26 for being throttled to 0.48MPa to participate in rectification;
2) Obtaining nitrogen with oxygen content less than 5ppm at the top of the tower after preliminary rectification by a lower tower 12, obtaining lean liquid air with oxygen content of 21% at the middle lower part of the lower tower 12, and obtaining oxygen-enriched liquid air with oxygen content of 37% at the bottom of the lower tower 12; nitrogen at the top of the lower tower 12 enters the condensing evaporator 13 through a fourteenth pipeline 114 to be condensed into liquid nitrogen, a part of the liquid nitrogen returns to the lower tower through a sixteenth pipeline 116 to be used as reflux liquid, a part of the liquid nitrogen enters the main heat exchanger 11 to be reheated to normal temperature after being pressurized to 2.2MPa through a liquid nitrogen pump 16 through a seventeenth pipeline 117 to be used as nitrogen products to exit the cryogenic separation cold box 27, another part of the liquid nitrogen enters the subcooler 15 through an eighteenth pipeline 118 to be subcooled, one part of the liquid nitrogen enters the top of the upper tower 14 to be used as reflux liquid of the upper tower after being throttled through a fourth throttle valve 25 through a nineteenth pipeline 119 to participate in rectification, and one part of the liquid nitrogen enters the cryogenic separation cold box 27 through a twentieth pipeline 120 to be used as liquid nitrogen products; the lean liquid air at the lower part of the lower tower 12 is supercooled by the cooler 15 and then divided into two parts, one part enters the upper middle part of the upper tower 14 to participate in rectification after being throttled by the second throttle valve 23 through the twelfth pipeline 112, and the other part enters the condenser of the refined argon tower 21 to serve as a cold source after being throttled by the third throttle valve 24 through the thirteenth pipeline 113; the oxygen-enriched liquid air in the tower bottom of the lower tower 12 enters an evaporator of the refined argon tower 21 through an eleventh pipeline 111 to be used as a heat source; part of liquid oxygen from the upper tower 14 is evaporated into oxygen in the condensation evaporator 13 to be used as ascending gas of the upper tower to participate in rectification, part of the oxygen is pressurized to 3.2MPa through a liquid oxygen pump through a twenty-first pipeline 121 and then enters the main heat exchanger 11 to be reheated to normal temperature to be used as oxygen product to be discharged from the cryogenic separation cold box 27, and part of the oxygen is used as liquid oxygen product to be discharged from the cryogenic separation cold box 27 through a twenty-second pipeline 122; low-pressure nitrogen is obtained at the top of the upper tower 14, the low-pressure nitrogen is reheated by the subcooler 15 and the main heat exchanger 11, then the low-pressure nitrogen is discharged after being subjected to regeneration gas by the air purification unit 3, a small part of oxygen is extracted at the bottom of the upper tower 14 as means for adjusting the argon content of the argon fraction, and the extracted oxygen is converged into a twenty-third pipeline 123 after passing through the subcooler through a twenty-fourth pipeline 124.
3) A certain amount of argon fraction containing 8% argon is pumped from the middle lower part of the upper tower 14, enters the bottom of a crude argon tower II 19 through a thirty-first pipeline 131, is pumped from the top after rectification and enters the bottom of a crude argon tower I18 through a thirty-second pipeline 132, liquid argon at the bottom of the crude argon tower I18 is pressurized to 0.95MPa through a thirty-third pipeline 133 by a circulating liquid argon pump 20 and then is sent to the upper part of the crude argon tower II 19 as reflux liquid to participate in rectification, and liquid in the tower kettle of the crude argon tower II 19 is returned to the argon fraction pumping position of the upper tower 14 through a thirty-fourth pipeline 134 to participate in rectification; the condenser cold source of the crude argon column I18 adopts an oxygen-enriched liquid space of a tower kettle of a lower tower 12 after throttling through an evaporator of a refined argon column 21 and a first throttle valve 22 by an eleventh pipeline 111, wherein a process argon part from the upper part of the crude argon column I18 is condensed, and the oxygen-enriched liquid space part is evaporated; the liquid argon at the bottom of the condenser of the crude argon column I18 flows back to the crude argon column I through a thirty-fifth pipeline 135 to be used as reflux liquid to participate in rectification, the process argon is sent to the middle part of the refined argon column 21 through a thirty-sixth pipeline 136 to participate in rectification, and the liquid air steam at the top of the condenser of the crude argon column I18 returns to the upper column 14 through a thirty-seventh pipeline 137; the condenser cold source of the refined argon tower 21 adopts lean liquid air throttled by the third throttle valve 24 through the thirteenth pipeline 113, the lean liquid air is evaporated into liquid air steam which is merged with liquid air steam of the thirty-seventh pipeline 137 through the thirty-eighth pipeline 138, partial process argon at the top of the condenser of the refined argon tower 21 is discharged out of the cryogenic separation cold box 27 through the thirty-ninth pipeline 139, the evaporator heat source of the refined argon tower 21 adopts oxygen-enriched liquid air of the tower bottom of the lower tower 12 through the eleventh pipeline 111, and pure liquid argon in the evaporator of the refined argon tower 21 is discharged out of the cryogenic separation cold box 27 through the fortieth pipeline 140.
The air booster 4 is provided with a middle extraction port, 2.8MPa of air at 40 ℃ extracted from the middle extraction port is divided into two streams, one stream sequentially passes through the pressurization of the low-temperature booster end 5, the cooling of the low-temperature booster end cooler 6, the pressurization of the high-temperature booster end 7 and the cooling of the high-temperature booster end cooler 8 through a fifth pipeline 105, enters the main heat exchanger 11 at the temperature of 40 ℃ and the pressure of 6.0MPa for cooling to-95 ℃ and then is extracted, then enters the expansion end 9 of the low-temperature expander for expansion to the pressure of 0.48MPa, enters the bottom of the lower tower 12 for rectification at the temperature of-173 ℃, enters the main heat exchanger 11 for cooling to 5 ℃ through a sixth pipeline 106, enters the expansion end 10 of the high-temperature expander for expansion to the pressure of 0.48MPa at the temperature of-84 ℃, then returns to the main heat exchanger 11 for further cooling to the temperature of-167 ℃ and enters the bottom of the lower tower 12 for rectification.
The bottom of the condenser of the crude argon column I18 is provided with a liquid-air reflux port, most liquid air flows back to the middle part of the upper column 14 through a forty-first pipeline 141 to participate in rectification, the upper part of the condenser of the crude argon column I18 is provided with a liquid-air overflow port, and part of liquid air overflows into the forty-first pipeline 141 through a forty-first pipeline 142.

Claims (5)

1. The utility model provides an air separation device that big liquid volume was prepared, includes air cleaner (1), air compressor (2), air purification unit (3), air booster (4), low temperature machine pressure boost end (5) and low temperature expander expansion end (9), low temperature machine pressure boost end cooler (6), high temperature machine pressure boost end (7) and high temperature expander expansion end (10), high temperature machine pressure boost end cooler (8) and cryogenic separation cold box unit (27), cryogenic separation cold box unit (27) include main heat exchanger (11), lower tower (12), condensation evaporator (13), go up tower (14), subcooler (15), liquid nitrogen pump (16), liquid oxygen pump (17), crude argon tower I (18), crude argon tower II (19), circulating liquid argon pump (20), smart argon tower (21), its characterized in that: the crude argon column I (18) comprises a column body and a condenser at the top of the column body, the refined argon column (21) comprises a column body, a condenser at the top of the column body and an evaporator at the bottom of the column body, the inlet of the air compressor (2) is input into the raw material atmosphere through an air filter (1), the outlet of the air compressor (2) is communicated with the inlet of the air purification unit (3) through a first pipeline (101), the outlet of the air purification unit (3) is respectively communicated with a second pipeline (102) and a third pipeline (103), the second pipeline (102) is communicated with the inlet at the bottom of the lower column (12) through the main heat exchanger (11), the third pipeline (103) is communicated with the inlet of the air booster (4), the outlet of the air booster (4) is communicated with the inlet at the lower part of the lower column (12) through a fourth pipeline (104) through the main heat exchanger (11) and an eighth throttle valve (26), the outlet of the lower argon column (12) is respectively communicated with the inlet of the lower column (12) through an eleventh pipeline (21), the evaporator (12) and a thirteenth pipeline (12) through the inlet of the lower pipeline (12), the twelfth pipeline (112) is communicated with the middle inlet of the upper tower (14) through a second throttle valve (23), the thirteenth pipeline (113) is communicated with the condenser inlet of the refined argon tower (21) through a third throttle valve (24), the top outlet of the lower tower (12) is communicated with the inlet of the condensation evaporator (13) through a fourteenth pipeline (114), the lower outlet of the condensation evaporator (13) is connected with a fifteenth pipeline (115), the fifteenth pipeline (115) is respectively communicated with a sixteenth pipeline (116), a seventeenth pipeline (117) and an eighteenth pipeline (118), the sixteenth pipeline (116) is communicated with the top inlet of the lower tower (12), the seventeenth pipeline (117) is communicated with the inlet of the upper tower (12) through a liquid nitrogen pump (16) and a main heat exchanger (11), the nineteenth pipeline (118) is respectively communicated with the inlet of the condensation evaporator (13) through a condenser (15), the nineteenth pipeline (119) is respectively communicated with the inlet of the twenty-first pipeline (13) through a nineteenth pipeline (119), the nineteenth pipeline (119) is respectively communicated with the outlet of the twenty-first heat exchanger (11) through a twenty-eighth pipeline (121), the twenty-first pipeline (121) is connected with the cryogenic separation cold box unit (27) through a liquid oxygen pump (17) and a main heat exchanger (11), the twenty-second pipeline (122) is connected with the cryogenic separation cold box unit (27), the top outlet of the upper tower (14) is communicated with a twenty-third pipeline (123), the twenty-third pipeline (123) is communicated with the air purification unit (3) through a cooler (15) and the main heat exchanger (11), the bottom of the upper tower (14) is connected with a twenty-fourth pipeline (124), the twenty-fourth pipeline (124) is in butt joint with the twenty-third pipeline (123), the outlet at the middle lower part of the upper tower (14) is communicated with the bottom inlet of the crude argon tower II (19) through a thirty-first pipeline (131), the top of the crude argon tower II (19) is communicated with the bottom of the crude argon tower I (18) through a thirty-second pipeline (132), the bottom of the crude argon tower I (18) is communicated with the bottom of the crude argon tower II (19) through a thirty-second pipeline (133) and the upper tower (19) through a thirty-fourth pipeline (136), the bottom outlet of the crude argon tower II (19) is communicated with the crude argon tower II (19) through a thirty-fourth pipeline (19), the thirty-fifth pipeline (135) is communicated with the upper part of the crude argon tower I (18), the thirty-sixth pipeline (136) is communicated with the middle part of the refined argon tower (21), the top of a condenser of the crude argon tower I (18) is communicated with an inlet in the middle part of the upper tower (14) through a thirty-seventh pipeline (137), the upper part of the condenser of the refined argon tower (21) is connected with a thirty-eighth pipeline (138), the thirty-eighth pipeline (138) is in butt joint with the thirty-seventh pipeline (137), the top of the condenser of the refined argon tower (21) is connected with a thirty-ninth pipeline (139), the thirty-ninth pipeline (139) is out of the cryogenic separation cold box unit (27), the bottom of an evaporator of the refined argon tower (21) is connected with a fortieth pipeline (140), and the fortieth pipeline (140) is out of the cryogenic separation cold box unit (27);
the lower tower (12) is a sieve plate tower or a structured packing tower, the upper tower (14), the crude argon tower I (18), the crude argon tower II (19) and the refined argon tower (21) are structured packing towers, and the main heat exchanger (11), the condensation evaporator (13), the subcooler (15), the crude argon tower I (18) condenser, the refined argon tower (21) evaporator and the condenser are all vacuum brazing plate-fin heat exchangers;
the air booster (4) is provided with a middle extraction port, the middle extraction port is respectively communicated with a fifth pipeline (105) and a sixth pipeline (106), the fifth pipeline (105) sequentially passes through the low-temperature machine booster end (5), the low-temperature machine booster end cooler (6), the high-temperature machine booster end (7), the high-temperature machine booster end cooler (8), the main heat exchanger (11), the low-temperature expansion machine expansion end (9) and the inlet at the bottom of the lower tower (12), the sixth pipeline (106) sequentially passes through the main heat exchanger (11) and the high-temperature expansion machine expansion end (10), and the main heat exchanger (11) is communicated with the inlet at the bottom of the lower tower (12).
2. A large liquid volume produced air separation unit as defined in claim 1 wherein: the bottom of the condenser of the crude argon column I (18) is provided with a liquid-air reflux port, the liquid-air reflux port is connected with a forty-first pipeline (141), the forty-first pipeline (141) is communicated with an inlet in the middle of the upper column (14), the upper part of the condenser of the crude argon column I (18) is provided with a liquid-air overflow port, the liquid-air overflow port is connected with a forty-second pipeline (142), and the forty-second pipeline (142) is communicated with the forty-first pipeline (141).
3. A method for large liquid volume production using the apparatus of claim 1 or 2, characterized in that: the method comprises the following steps:
step 1), the raw material of the device is air, the air is filtered by an air filter (1) and then enters an air compressor (2) for compression, the pressure of the compressed air is 0.5MPa, and then enters an air purification unit (3) through a first pipeline (101) to remove CO 2 、H 2 O and part of hydrocarbon are divided into two parts, one part enters a main heat exchanger (11) through a second pipeline (102) and is cooled to about-167 ℃, then enters the bottom of a lower tower (12) from the main heat exchanger (11) to participate in rectification, the other part enters an air booster (4) through a third pipeline (103) to boost pressure, enters the liquid space of the main heat exchanger (11) through a fourth pipeline (104) after the final stage of boosting pressure is 6.0MPa, is cooled to about-167 ℃, and then enters the middle lower part of the lower tower (12) to participate in rectification through a throttle valve (26) to be throttled to 0.48 MPa;
step 2), obtaining nitrogen with oxygen content less than 5ppm at the top of the tower after preliminary rectification by a lower tower (12), obtaining lean liquid air with oxygen content of 21% at the middle lower part of the lower tower, obtaining oxygen-enriched liquid air with oxygen content of 37% at the bottom of the lower tower, enabling nitrogen at the top of the lower tower (12) to enter a condensing evaporator (13) through a fourteenth pipeline (114) to be condensed into liquid nitrogen, enabling a part of the liquid nitrogen to return to the lower tower (12) through a sixteenth pipeline (116) to serve as reflux liquid, enabling the liquid nitrogen to enter a main heat exchanger (11) after being pressurized to 2.2MPa through a seventeenth pipeline (117) and then being reheated to be taken as nitrogen product, enabling the other part of the liquid nitrogen to enter a subcooler (15) through an eighteenth pipeline (118), enabling the first part of the liquid nitrogen to enter the top of the upper tower (14) through a nineteenth pipeline (119) after being throttled through a fourth throttle valve (25) to be taken as reflux liquid of the upper tower (14), enabling the first part of the liquid nitrogen to enter the upper tower to be taken as reflux liquid of the upper tower (14), enabling the liquid nitrogen to enter the second part of the main heat exchanger (11) to enter the main heat exchanger (11) through a seventeenth pipeline (117) to be taken as reflux liquid of the main heat exchanger (27), enabling the second part of the liquid nitrogen product to enter the upper part of the main heat exchanger (21) through the main heat exchanger (15) to be throttled by the second pipeline (21) after entering the upper part of the upper tower (112) through the nineteenth pipeline (23) through the throttle valve (23), oxygen-enriched liquid air at the tower bottom of the lower tower (12) enters an evaporator of the refined argon tower (21) through an eleventh pipeline (111) to serve as a heat source, part of liquid oxygen from the upper tower (14) is evaporated into oxygen in a condensation evaporator (13) to serve as ascending gas of the upper tower (14) to participate in rectification, part of the oxygen is pressurized to 3.2MPa through a liquid oxygen pump through a twenty-first pipeline (121) and enters a main heat exchanger (11) to be reheated to normal temperature to serve as an oxygen product to be discharged out of a cryogenic separation cold box unit (27), part of the oxygen is taken as a liquid oxygen product to be discharged out of the cryogenic separation cold box unit (27) through a twenty-second pipeline (122), low-pressure nitrogen is obtained at the top of the upper tower (14), the low-pressure nitrogen is reheated through a subcooler (15) and the main heat exchanger (11) to be discharged after the air purification unit (3) is used as regeneration gas, a small part of the oxygen is pumped out at the bottom of the upper tower (14) to serve as a means for adjusting the argon content of fraction, and the pumped oxygen is converged into a twenty-third pipeline (123) after passing through the subcooler (15);
step 3), pumping a certain amount of argon fraction containing 8% argon from the middle lower part of the upper tower (14), entering the bottom of a crude argon tower II (19) through a thirty-first pipeline (131), pumping the argon fraction from the top after rectification, entering the bottom of a crude argon tower I (18) through a thirty-second pipeline (132), pressurizing liquid argon at the bottom of the crude argon tower I (18) to 0.95MPa through a thirty-third pipeline (133) through a circulating liquid argon pump (20), sending the liquid argon to the upper part of the crude argon tower II (19) as reflux liquid to participate in rectification, and returning the liquid in the tower kettle of the crude argon tower II (19) to the argon fraction pumping position of the upper tower (14) through a thirty-fourth pipeline (134) to participate in rectification; the condenser cold source of the crude argon column I (18) adopts an oxygen-enriched liquid air which is throttled by an eleventh pipeline (111) through an evaporator of the refined argon column (21) and a first throttle valve (22) to be used as reflux liquid for rectification, wherein a process argon part from the upper part of the crude argon column I (18) is condensed, the oxygen-enriched liquid air part is evaporated, liquid argon at the bottom of the condenser of the crude argon column I (18) flows back to the crude argon column I through a thirty-fifth pipeline (135) to be used as reflux liquid for rectification, the process argon is sent to the middle part of the refined argon column (21) through a thirty-sixth pipeline (136) to be used for rectification, liquid air steam at the top of the condenser of the crude argon column I (18) is returned to the upper column (14) through a thirty-seventh pipeline (137), the liquid air of the condenser of the refined argon column (21) adopts a lean liquid air which is throttled by a third throttle valve (24) through a thirteenth pipeline (113), the lean liquid air steam is evaporated into liquid air steam which is mixed with liquid air steam of a thirty-seventh pipeline (137) through a thirty-eighth pipeline (138), the liquid air steam at the top of the condenser of the refined argon column I (21) is sent out of the pure argon column (21) through a thirty-seventh pipeline (27) to be used as cold air source through a cold air unit of the evaporator of the refined argon (21) through a thirty-seventh pipeline (27).
4. A method of large liquid volume production according to claim 3, wherein: the air booster (4) is provided with a middle extraction port, the air with the temperature of 2.8MPa and 40 ℃ extracted from the middle extraction port is divided into two streams, one stream is sequentially subjected to supercharging at the low-temperature booster end (5), cooling at the low-temperature booster end cooler (6), supercharging at the high-temperature booster end (7) and cooling at the high-temperature booster end cooler (8) through a fifth pipeline (105), enters the main heat exchanger (11) at the temperature of 40 ℃ and the pressure of 6.0MPa, is cooled to-95 ℃ and is extracted, then enters the expansion end (9) of the low-temperature expander and is expanded to the pressure of 0.48MPa and the temperature of-173 ℃ and enters the bottom of the lower tower (12) to participate in rectification, and the other stream is extracted from the middle of the main heat exchanger and enters the expansion end (10) of the high-temperature expander and is expanded to the pressure of 0.48MPa and the temperature of-84 ℃ after entering the main heat exchanger (11) through a sixth pipeline (106) to be cooled to the bottom of the lower tower (12) to participate in rectification after the expansion at the temperature of-167 ℃.
5. A method of large liquid volume production according to claim 3, wherein: a liquid-air reflux port is arranged at the bottom of the condenser of the crude argon column I (18), most liquid air flows back to the middle part of the upper column through a forty-first pipeline (141) to participate in rectification, a liquid-air overflow port is arranged at the upper part of the condenser of the crude argon column I (18), and part of liquid air overflows into the forty-first pipeline (141) through a forty-second pipeline (142).
CN201810765000.9A 2018-07-12 2018-07-12 Air separation device and method for preparing large liquid volume Active CN108759311B (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
CN201810765000.9A CN108759311B (en) 2018-07-12 2018-07-12 Air separation device and method for preparing large liquid volume

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
CN201810765000.9A CN108759311B (en) 2018-07-12 2018-07-12 Air separation device and method for preparing large liquid volume

Publications (2)

Publication Number Publication Date
CN108759311A CN108759311A (en) 2018-11-06
CN108759311B true CN108759311B (en) 2023-10-03

Family

ID=63973423

Family Applications (1)

Application Number Title Priority Date Filing Date
CN201810765000.9A Active CN108759311B (en) 2018-07-12 2018-07-12 Air separation device and method for preparing large liquid volume

Country Status (1)

Country Link
CN (1) CN108759311B (en)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN109186179B (en) * 2018-09-30 2023-09-19 苏州制氧机股份有限公司 Full-rectification argon extraction oxygen-enriched air separation device and process
CN109323534A (en) * 2018-11-06 2019-02-12 杭州杭氧股份有限公司 It is a kind of that high pressure oxygen method and device is produced by cryogenic rectification method purification air
CN113670003B (en) * 2021-07-29 2022-08-09 北京科技大学 High-safety energy storage, power generation and substance recovery external compression air separation process flow
CN113623941B (en) * 2021-08-11 2022-08-26 乔治洛德方法研究和开发液化空气有限公司 Air separation unit suitable for retrofitting and method for retrofitting the air separation unit

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5533339A (en) * 1994-05-27 1996-07-09 The Boc Group Plc Air separation
CN102230716A (en) * 2011-06-08 2011-11-02 杭州优埃基空分设备有限公司 Method and device for separating air through air pressurization, backflow expansion and internal compression
CN204115392U (en) * 2014-08-29 2015-01-21 中国空分设备有限公司 With the full air separation units producing liquids of air supply compressor
CN104390427A (en) * 2014-10-21 2015-03-04 杭州福斯达实业集团有限公司 High-temperature and low-temperature expansion energy-saving nitrogen production device and nitrogen production method
CN104807290A (en) * 2015-04-29 2015-07-29 河南开元空分集团有限公司 Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion
CN105823302A (en) * 2016-05-18 2016-08-03 杭州杭氧股份有限公司 Air separation device and method capable of achieving oxygen inner and outer compression procedure interchange

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5533339A (en) * 1994-05-27 1996-07-09 The Boc Group Plc Air separation
CN102230716A (en) * 2011-06-08 2011-11-02 杭州优埃基空分设备有限公司 Method and device for separating air through air pressurization, backflow expansion and internal compression
CN204115392U (en) * 2014-08-29 2015-01-21 中国空分设备有限公司 With the full air separation units producing liquids of air supply compressor
CN104390427A (en) * 2014-10-21 2015-03-04 杭州福斯达实业集团有限公司 High-temperature and low-temperature expansion energy-saving nitrogen production device and nitrogen production method
CN104807290A (en) * 2015-04-29 2015-07-29 河南开元空分集团有限公司 Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion
CN105823302A (en) * 2016-05-18 2016-08-03 杭州杭氧股份有限公司 Air separation device and method capable of achieving oxygen inner and outer compression procedure interchange

Also Published As

Publication number Publication date
CN108759311A (en) 2018-11-06

Similar Documents

Publication Publication Date Title
CN108759311B (en) Air separation device and method for preparing large liquid volume
CN111141110B (en) Low-energy-consumption medium-pressure nitrogen preparation process
CN109186179B (en) Full-rectification argon extraction oxygen-enriched air separation device and process
WO2021043182A1 (en) Air separation apparatus and method using lng cold energy
CN204115392U (en) With the full air separation units producing liquids of air supply compressor
CN201377961Y (en) Multi-operating mode air separation equipment
CN104807290A (en) Device and method for preparing low-pressure nitrogen gas by using single-tower double-backflow expansion
CN109084528B (en) Cryogenic air separation system with newly-added nitrogen tower
CN113686099B (en) Material recovery method based on internal compression air separation energy storage device
CN205373261U (en) Low positive pressure of low high extraction percentage of liquid flows large -scale interior compression air separation system of inflation
CN105066586B (en) Device for preparing raw material gas for synthetic ammonia and L NG by liquid nitrogen washing and preparation method thereof
CN208443098U (en) The air separation unit that big amount of liquid is produced
CN215766044U (en) Air separation device for preparing full liquid in nitrogen circulation process
CN112229143A (en) Device and method for producing oxygen and nitrogen by separating air through cryogenic rectification
CN109323533B (en) Method and device for reducing space division energy consumption by using medium-pressure rectifying tower
CN204594094U (en) The two stream backed expansion of single tower produces the device of low-pressure nitrogen
CN112304027A (en) Air separation device for nitrogen circulation flow full liquid preparation and preparation method
CN208186973U (en) A kind of large size cryogenic air separation plant
CN203687518U (en) Low-purity oxygen preparing device with auxiliary rectifying tower
CN201377962Y (en) Equipment producing compressed natural gas from mixed gas containing methane
CN1038514A (en) Produce the air separating technological of hyperbaric oxygen and elevated pressure nitrogen
CN100443838C (en) Method and equipment for separating stream backed expansion air
CN114791204A (en) Nitrogen circulating low-temperature rectification crude argon purification and liquefaction device and use method thereof
CN213578367U (en) Device for producing oxygen and nitrogen by separating air through cryogenic rectification
CN100357684C (en) Method and device for separating air

Legal Events

Date Code Title Description
PB01 Publication
PB01 Publication
SE01 Entry into force of request for substantive examination
SE01 Entry into force of request for substantive examination
GR01 Patent grant
GR01 Patent grant