CN111322832A - Full liquid air separation plant and process - Google Patents

Full liquid air separation plant and process Download PDF

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Publication number
CN111322832A
CN111322832A CN202010165585.8A CN202010165585A CN111322832A CN 111322832 A CN111322832 A CN 111322832A CN 202010165585 A CN202010165585 A CN 202010165585A CN 111322832 A CN111322832 A CN 111322832A
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China
Prior art keywords
heat exchanger
low
heat exchange
main heat
exchange pipeline
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Pending
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CN202010165585.8A
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Chinese (zh)
Inventor
薛鲁
马昆
贾盛兰
周发州
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Suzhou Xinglu Air Separation Plant Science And Technology Development Co ltd
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Suzhou Xinglu Air Separation Plant Science And Technology Development Co ltd
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Priority to CN202010165585.8A priority Critical patent/CN111322832A/en
Publication of CN111322832A publication Critical patent/CN111322832A/en
Priority to PCT/CN2021/079018 priority patent/WO2021179980A1/en
Priority to US17/930,489 priority patent/US20230003445A1/en
Pending legal-status Critical Current

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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
    • F25J3/04636—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 hybrid air separation unit, e.g. combined process by cryogenic separation and non-cryogenic separation techniques
    • 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
    • F25J3/04163—Hot end purification of the feed air
    • F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
    • F25J3/04181—Regenerating the adsorbents
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04339—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 air
    • F25J3/04345—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 air and comprising a gas work expansion loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/60—Processes or apparatus using other separation and/or other processing means using adsorption on solid adsorbents, e.g. by temperature-swing adsorption [TSA] at the hot or cold end
    • F25J2205/66—Regenerating the adsorption vessel, e.g. kind of reactivation gas
    • F25J2205/70—Heating the adsorption 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
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/58—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
    • 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
    • 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

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

Abstract

The invention relates to an all-liquid air separation plant, which comprises an air filtering, compressing, precooling and purifying system, a high-temperature expansion machine, a low-temperature expansion machine, a main heat exchanger and a rectifying system. The air is filtered, compressed, precooled and purified and then sent to the pressurization side of the high-temperature expansion machine, the pressurization side of the low-temperature expansion machine and the main branch after main exchange are divided into two branches which are respectively connected with the expansion side of the low-temperature expansion machine and the rectification system, the expansion side of the low-temperature expansion machine is divided into two branches which are respectively connected with the main heat exchanger and the rectification system, the main heat exchanger is connected with the expansion side of the high-temperature expansion machine again, the expansion side of the high-temperature expansion machine is connected with the main heat exchanger again, the main heat exchanger is connected with the purification system again to provide adsorbent regeneration gas, a low-pressure dirty nitrogen gas outlet and a low-pressure nitrogen gas outlet of the rectification. The invention has simple configuration, convenient implementation, higher air separation efficiency and lower energy consumption.

Description

Full liquid air separation plant and process
Technical Field
The invention belongs to the technical field of air separation, and particularly relates to full-liquid air separation equipment and a process.
Background
In the existing air separation equipment and the matching process, a plurality of compressors are generally needed to be used for refrigeration and realize air circulation, refrigeration equipment is generally needed to be arranged to provide refrigeration capacity, and the defects of low efficiency and high energy consumption exist.
Disclosure of Invention
The invention aims to provide an all-liquid air separation plant with higher efficiency and lower energy consumption.
In order to achieve the purpose, the invention adopts the technical scheme that:
an all-liquid air separation plant comprises an air filtering system, a compression system, a precooling system, a purification system, a high-temperature expander, a low-temperature expander, a main heat exchanger and a rectification system for rectifying air;
air is sent to a pressure increasing side of the high-temperature expansion machine through the air filtering system, the compression system, the precooling system and the purification system, the pressure increasing side of the high-temperature expansion machine is connected with the pressure increasing side of the low-temperature expansion machine, the pressure increasing side of the low-temperature expansion machine is connected with a first heat exchange pipeline in the main heat exchanger, the first heat exchange pipeline in the main heat exchanger comprises a main pipeline connected with the pressure increasing side of the low-temperature expansion machine and two branches branched from the main pipeline, one branch is connected with an expansion side of the low-temperature expansion machine, the other branch is connected with the rectification system, the expansion side of the low-temperature expansion machine is divided into two branches and respectively connected with a second heat exchange pipeline in the main heat exchanger and the rectification system, and the rectification system extracts a strand of pressure sewage nitrogen and merges into a second heat exchange pipeline in the main heat exchanger, a second heat exchange pipeline in the main heat exchanger is connected with the expansion side of the high-temperature expansion machine, the expansion side of the high-temperature expansion machine is connected with a third heat exchange pipeline in the main heat exchanger, the outlet of the third heat exchange pipeline in the main heat exchanger is divided into two paths, one path is connected with the purification system to provide adsorbent regeneration gas, and the other path is connected with the precooling system; and a low-pressure waste nitrogen output port of the rectification system is connected with a fourth heat exchange pipeline in the main heat exchanger, a low-pressure nitrogen outlet of the rectification system is connected with a fifth heat exchange pipeline in the main heat exchanger, and the fourth heat exchange pipeline and the fifth heat exchange pipeline in the main heat exchanger are jointly connected with the precooling system.
The invention also provides an all-liquid air separation process adopted by the all-liquid air separation equipment, wherein the all-liquid air separation process comprises the following steps: after being filtered, compressed, precooled and purified, the air enters a first heat exchange pipeline in the main heat exchanger for heat exchange after being continuously pressurized by a pressurizing side of the high-temperature expander and a pressurizing side of the low-temperature expander, a part of air in the first heat exchange pipeline in the main heat exchanger is pumped out in the middle of the main heat exchanger and enters an expansion end of the low-temperature expander for expansion, and the other part of air becomes high-pressure liquid air at the bottom of the main heat exchanger and enters the rectification system; the air expanded by the expansion end of the low-temperature expansion machine enters a second heat exchange pipeline in the main heat exchanger for heat exchange and is rectified by the rectification system respectively in two ways; the rectification system extracts a strand of pressure sewage nitrogen and merges the pressure sewage nitrogen into a second heat exchange pipeline in the main heat exchanger, the sewage nitrogen mixed and subjected to heat exchange through the second heat exchange pipeline in the main heat exchanger enters the expansion end of the high-temperature expansion machine to be expanded into low-pressure sewage nitrogen, and the low-pressure sewage nitrogen is reheated through a third heat exchange pipeline in the main heat exchanger to become low-pressure normal-temperature sewage nitrogen; part of the low-pressure normal-temperature waste nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part of the low-pressure normal-temperature waste nitrogen enters the precooling system; the low-pressure sewage nitrogen generated by the rectification system is reheated by a fourth heat exchange pipeline in the main heat exchanger, the low-pressure nitrogen generated by the rectification system is reheated by a fifth heat exchange pipeline in the main heat exchanger, and the sewage nitrogen reheated by the fourth heat exchange pipeline in the main heat exchanger and the nitrogen reheated by the fifth heat exchange pipeline in the main heat exchanger are jointly connected to enter the precooling system.
Preferably, the air is compressed and cooled in the compressor to 35bar, 40 ℃.
Preferably, the air is further cooled to 10-15 ℃ in the chilled water heat exchanger.
Preferably, air enters the medium pressure purification system to remove water and carbon dioxide.
Preferably, the high-pressure liquid air enters the rectification system after being throttled.
Preferably, the rectification system separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon.
Due to the application of the technical scheme, compared with the prior art, the invention has the following advantages: the invention has simple configuration, convenient implementation, high air separation efficiency, high oxygen extraction rate and low energy consumption.
Drawings
FIG. 1 is a process flow diagram of an all liquid air separation plant of the present invention.
In the above drawings: 1. a filtration, compression, pre-cooling, purification system (including an air filtration system, a compression system, a pre-cooling system, a purification system); 2. a high temperature expander; 3. a low temperature expander; 4. a primary heat exchanger; 5. a rectification system.
Detailed Description
The invention will be further described with reference to examples of embodiments shown in the drawings to which the invention is attached.
The first embodiment is as follows: as shown in fig. 1, an all-liquid air separation plant comprises an air filtering, compressing, precooling and purifying system 1, a high-temperature expander 2, a low-temperature expander 3, a main heat exchanger 4 and a rectifying system 5 for rectifying air.
Air is sent to the pressure increasing side of a high-temperature expansion machine 2 through an air filtering, compressing, precooling and purifying system 1 (namely, the air passes through the air filtering system, the compressing system, the precooling system and the purifying system in sequence), the pressure increasing side of the high-temperature expansion machine 2 is connected with the pressure increasing side of a low-temperature expansion machine 3, the pressure increasing side of the low-temperature expansion machine 3 is connected with a first heat exchange pipeline in a main heat exchanger 4, the first heat exchange pipeline in the main heat exchanger 4 comprises a main pipeline connected with the pressure increasing side of the low-temperature expansion machine 3 and two branch pipelines branched from the main pipeline, one branch pipeline is connected with the expansion side of the low-temperature expansion machine 3, and the other branch pipeline is connected with a rectifying. The expansion side of the low-temperature expansion machine 3 is divided into two paths to be respectively connected with a second heat exchange pipeline in the main heat exchanger 4 and the rectification system 5, and the rectification system extracts a stream of pressure waste nitrogen and feeds the pressure waste nitrogen into the second heat exchange pipeline in the main heat exchanger 4. The second heat exchange pipeline in the main heat exchanger 4 is connected with the expansion side of the high-temperature expansion machine 2, and the pressure sewage nitrogen becomes low-pressure sewage nitrogen through the high-temperature expansion machine 2. The expansion side of the high-temperature expansion machine 2 is connected with a third heat exchange pipeline in the main heat exchanger 8, the outlet of the third heat exchange pipeline in the main heat exchanger 4 is divided into two paths, one path is connected with the purification system to provide adsorbent regenerated gas, and the other path is connected with the precooling system. Namely, the low-pressure sewage nitrogen is reheated by a third heat exchange pipeline in the main heat exchanger 4 to become low-pressure normal-temperature sewage nitrogen, one part of the low-pressure normal-temperature sewage nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part of the low-pressure normal-temperature sewage nitrogen is connected with the precooling system to participate in the preparation of chilled water. A low-pressure sewage nitrogen output port of the rectification system 5 is connected with a fourth heat exchange pipeline in the main heat exchanger 4, a low-pressure nitrogen outlet of the rectification system 5 is connected with a fifth heat exchange pipeline in the main heat exchanger 4, and the fourth heat exchange pipeline and the fifth heat exchange pipeline in the main heat exchanger 4 are connected with the precooling system together.
An all-liquid air separation process based on the all-liquid air separation plant comprises the following steps: the air is filtered, compressed, precooled and purified to become the purified compressed air with the pressure of 10-60 bar and the temperature of 5-50 ℃. The purified compressed air is continuously pressurized by the pressurization side of the high-temperature expander 2 and the pressurization side of the low-temperature expander 3, then enters a first heat exchange pipeline in the main heat exchanger 4 for heat exchange, a part of air in the first heat exchange pipeline in the main heat exchanger 4 is pumped out in the middle of the main heat exchanger 4 and enters the expansion end of the low-temperature expander 3 for expansion, and the other part of air becomes high-pressure liquid air at the bottom of the main heat exchanger 4 and enters the rectification system 5 after throttling. The air expanded by the expansion end of the low-temperature expansion machine 3 is divided into two paths, one path enters a second heat exchange pipeline in the main heat exchanger 4 for heat exchange, and the other path enters the rectification system 5 for rectification. The rectification system 5 extracts a stream of pressure sewage nitrogen, the pressure sewage nitrogen is merged into a second heat exchange pipeline in the main heat exchanger 4, the sewage nitrogen mixed and subjected to heat exchange through the second heat exchange pipeline in the main heat exchanger 4 enters the expansion end of the high-temperature expansion machine 3 to be expanded into low-pressure sewage nitrogen, and the low-pressure sewage nitrogen is reheated through a third heat exchange pipeline in the main heat exchanger 4 to be changed into low-pressure normal-temperature sewage nitrogen. And one part of low-pressure normal-temperature waste nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part of low-pressure normal-temperature waste nitrogen enters the precooling system to participate in the preparation of chilled water. The rectification system 5 separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon, and generates low-pressure sewage nitrogen and low-pressure nitrogen. The low-pressure sewage nitrogen generated by the rectification system 5 is reheated by a fourth heat exchange pipeline in the main heat exchanger 4, the low-pressure nitrogen generated by the rectification system 5 is reheated by a fifth heat exchange pipeline in the main heat exchanger 4, and the sewage nitrogen reheated by the fourth heat exchange pipeline in the main heat exchanger 4 and the low-pressure nitrogen reheated by the fifth heat exchange pipeline in the main heat exchanger 4 are jointly connected to enter a precooling system to prepare chilled water.
In the scheme, the method comprises the following steps:
1. the compressed air after filtration, compression, precooling and purification enters the pressurization sides of the high-temperature expansion machine 2 and the low-temperature expansion machine 3 for continuous pressurization, then enters the main heat exchanger 4 for heat exchange, and then enters the high-temperature expansion machine 2 for expansion after the air is expanded by the low-temperature expansion machine 3, is mixed with pressure contaminated nitrogen in the main heat exchanger 4 for reheating, and then enters the main heat exchanger 4 for reheating to become low-pressure normal-temperature contaminated nitrogen, namely the high-temperature expansion machine 2 and the low-temperature expansion machine 3 are combined under the conditions of high pressure and high temperature to carry out high-efficiency expansion refrigeration by utilizing the high-temperature high enthalpy principle.
The above embodiments are merely illustrative of the technical ideas and features of the present invention, and the purpose thereof is to enable those skilled in the art to understand the contents of the present invention and implement the present invention, and not to limit the protection scope of the present invention. All equivalent changes and modifications made according to the spirit of the present invention should be covered within the protection scope of the present invention.

Claims (7)

1. An all-liquid air separation plant, characterized in that: the full-liquid air separation equipment comprises an air filtering system, a compression system, a precooling system, a purification system, a high-temperature expansion machine, a low-temperature expansion machine, a main heat exchanger and a rectification system for rectifying air;
air is sent to a pressure increasing side of the high-temperature expansion machine through the air filtering system, the compression system, the precooling system and the purification system, the pressure increasing side of the high-temperature expansion machine is connected with the pressure increasing side of the low-temperature expansion machine, the pressure increasing side of the low-temperature expansion machine is connected with a first heat exchange pipeline in the main heat exchanger, the first heat exchange pipeline in the main heat exchanger comprises a main pipeline connected with the pressure increasing side of the low-temperature expansion machine and two branches branched from the main pipeline, one branch is connected with an expansion side of the low-temperature expansion machine, the other branch is connected with the rectification system, the expansion side of the low-temperature expansion machine is divided into two branches and respectively connected with a second heat exchange pipeline in the main heat exchanger and the rectification system, and the rectification system extracts a strand of pressure sewage nitrogen and merges into a second heat exchange pipeline in the main heat exchanger, a second heat exchange pipeline in the main heat exchanger is connected with the expansion side of the high-temperature expansion machine, the expansion side of the high-temperature expansion machine is connected with a third heat exchange pipeline in the main heat exchanger, the outlet of the third heat exchange pipeline in the main heat exchanger is divided into two paths, one path is connected with the purification system to provide adsorbent regeneration gas, and the other path is connected with the precooling system; and a low-pressure waste nitrogen output port of the rectification system is connected with a fourth heat exchange pipeline in the main heat exchanger, a low-pressure nitrogen outlet of the rectification system is connected with a fifth heat exchange pipeline in the main heat exchanger, and the fourth heat exchange pipeline and the fifth heat exchange pipeline in the main heat exchanger are jointly connected with the precooling system.
2. An all-liquid air separation process realized based on the all-liquid air separation plant according to claim 1, characterized in that: the full-liquid air separation process comprises the following steps: after being filtered, compressed, precooled and purified, the air enters a first heat exchange pipeline in the main heat exchanger for heat exchange after being continuously pressurized by a pressurizing side of the high-temperature expander and a pressurizing side of the low-temperature expander, a part of air in the first heat exchange pipeline in the main heat exchanger is pumped out in the middle of the main heat exchanger and enters an expansion end of the low-temperature expander for expansion, and the other part of air becomes high-pressure liquid air at the bottom of the main heat exchanger and enters the rectification system; the air expanded by the expansion end of the low-temperature expansion machine enters a second heat exchange pipeline in the main heat exchanger for heat exchange and is rectified by the rectification system respectively in two ways; the rectification system extracts a strand of pressure sewage nitrogen and merges the pressure sewage nitrogen into a second heat exchange pipeline in the main heat exchanger, the sewage nitrogen mixed and subjected to heat exchange through the second heat exchange pipeline in the main heat exchanger enters the expansion end of the high-temperature expansion machine to be expanded into low-pressure sewage nitrogen, and the low-pressure sewage nitrogen is reheated through a third heat exchange pipeline in the main heat exchanger to become low-pressure normal-temperature sewage nitrogen; part of the low-pressure normal-temperature waste nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part of the low-pressure normal-temperature waste nitrogen enters the precooling system; the low-pressure sewage nitrogen generated by the rectification system is reheated by a fourth heat exchange pipeline in the main heat exchanger, the low-pressure nitrogen generated by the rectification system is reheated by a fifth heat exchange pipeline in the main heat exchanger, and the sewage nitrogen reheated by the fourth heat exchange pipeline in the main heat exchanger and the nitrogen reheated by the fifth heat exchange pipeline in the main heat exchanger are jointly connected to enter the precooling system.
3. The all-liquid air separation process of claim 4, wherein: the air is compressed and cooled in the compressor to 35bar, 40 ℃.
4. The all-liquid air separation process of claim 4, wherein: and further cooling the air to 10-15 ℃ in the chilled water heat exchanger.
5. The all-liquid air separation process of claim 4, wherein: air enters the medium pressure purification system to remove water and carbon dioxide.
6. The all-liquid air separation process of claim 4, wherein: and the high-pressure liquid air enters the rectification system after being throttled.
7. The all-liquid air separation process of claim 4, wherein: and the rectification system is used for separating and liquefying to obtain liquid nitrogen, liquid oxygen and liquid argon.
CN202010165585.8A 2020-03-11 2020-03-11 Full liquid air separation plant and process Pending CN111322832A (en)

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