WO2021179980A1 - Fully-liquefied gas separation equipment and process - Google Patents

Fully-liquefied gas separation equipment and process Download PDF

Info

Publication number
WO2021179980A1
WO2021179980A1 PCT/CN2021/079018 CN2021079018W WO2021179980A1 WO 2021179980 A1 WO2021179980 A1 WO 2021179980A1 CN 2021079018 W CN2021079018 W CN 2021079018W WO 2021179980 A1 WO2021179980 A1 WO 2021179980A1
Authority
WO
WIPO (PCT)
Prior art keywords
heat exchanger
low
heat exchange
main heat
pressure
Prior art date
Application number
PCT/CN2021/079018
Other languages
French (fr)
Chinese (zh)
Inventor
薛鲁
马昆
贾盛兰
周发州
Original Assignee
苏州市兴鲁空分设备科技发展有限公司
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 苏州市兴鲁空分设备科技发展有限公司 filed Critical 苏州市兴鲁空分设备科技发展有限公司
Publication of WO2021179980A1 publication Critical patent/WO2021179980A1/en
Priority to US17/930,489 priority Critical patent/US20230003445A1/en

Links

Images

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
    • F25J3/04636—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

Definitions

  • the invention belongs to the field of air separation technology (the technology for separating various components from the air), and specifically relates to an all-liquid air separation equipment and process.
  • the purpose of the present invention is to provide an all-liquid air separation plant with higher efficiency and lower energy consumption.
  • An all-liquid air separation equipment including an air filtration system, a compression system, a pre-cooling system, a purification system, a high-temperature expander, a low-temperature expander, a main heat exchanger, and a rectification system for rectifying air;
  • the air filtration system, the compression system, the pre-cooling system, and the purification system are connected in sequence and then connected to the supercharging side of the high temperature expander, and the supercharging side of the high temperature expander is connected to the low temperature
  • the supercharging side of the expander, the supercharging side of the low-temperature expander is connected to the first heat exchange pipeline in the main heat exchanger, and the first heat exchange pipeline in the main heat exchanger includes The main circuit connected to the supercharging side of the low-temperature expander and two branch circuits branched from the main circuit, one of the branch circuits is connected to the expansion side of the low-temperature expander, and the other branch is connected to
  • the expansion side of the low-temperature expander is connected to the second heat exchange pipeline in the main heat exchanger and the rectification system in two paths, and the rectification system extracts one
  • the sewage nitrogen pipeline of the pressure sewage nitrogen is merged into the second heat exchange pipeline in the main heat exchanger, and the second heat exchange pipeline in
  • the present invention also provides an all-liquid air separation process adopted by the above-mentioned all-liquid air separation equipment.
  • the all-liquid air separation process is as follows: after air is filtered, compressed, pre-cooled, and purified, it passes through the pressurizing side of the high-temperature expander and After the pressurization side of the low-temperature expander is continuously pressurized, it enters the first heat exchange pipeline in the main heat exchanger to exchange heat, and the heat exchange in the first heat exchange pipeline in the main heat exchanger Part of the air is drawn out in the middle of the main heat exchanger and enters the expansion end of the low-temperature expander to expand, and another part of the air becomes high-pressure liquid at the bottom of the main heat exchanger and enters the rectification system; The air expanded at the expansion end of the cryogenic expander enters the second heat exchange pipe in the main heat exchanger in two ways for heat exchange and rectification by the rectification system; the rectification system draws one The pressurized sewage nitrogen is merged into the second heat
  • the expansion end of the high-temperature expander expands into low-pressure sewage nitrogen, and the low-pressure sewage nitrogen is reheated by the third heat exchange pipe in the main heat exchanger to become low-pressure normal-temperature sewage nitrogen; part of the low-pressure normal-temperature sewage nitrogen enters the plant
  • the purification system provides adsorbent regeneration gas for the purification system, and another part of the low-pressure normal temperature polluted nitrogen enters the pre-cooling system; the low-pressure polluted nitrogen generated by the rectification system passes through the second in the main heat exchanger Four heat exchange pipes are reheated.
  • the low-pressure nitrogen generated by the rectification system is reheated by the fifth heat exchange pipe in the main heat exchanger, and is exchanged by the fourth heat exchange pipe in the main heat exchanger.
  • the reheated waste nitrogen gas of the heat pipe and the reheated nitrogen gas of the fifth heat exchange pipe in the main heat exchanger are connected together to enter the pre-cooling system.
  • the air is filtered, compressed, pre-cooled, purified to remove water and carbon dioxide into compressed air with a pressure of 10-60 bar and a temperature of 5-50°C.
  • air enters the medium pressure purification system to remove water and carbon dioxide.
  • the high-pressure liquid air enters the rectification system after throttling.
  • the rectification system separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon.
  • the present invention has the following advantages compared with the prior art: the present invention is simple in configuration, easy to implement, and has high air separation efficiency, high oxygen extraction rate, and low energy consumption.
  • Figure 1 is a process flow diagram of the all-liquid air separation plant of the present invention.
  • Embodiment 1 As shown in Figure 1, an all-liquid air separation plant includes air filtration, compression, pre-cooling, purification system 1, high temperature expander 2, low temperature expander 3, main heat exchanger 4, and Distillation system for rectifying air5.
  • the expanders including the high-temperature expander 2 and the low-temperature expander 3, each have an expansion side for expanding the gas to depressurize it and a supercharging side for compressing the gas to pressurize it, that is, the high-temperature expander 2 has a high-temperature expander
  • the expansion side 21 and the supercharging side 22 of the high temperature expander, the low temperature expander 3 has the expansion side 31 of the low temperature expander and the supercharging side 32 of the low temperature expander.
  • the air filtration, compression, pre-cooling, and purification system 1 (that is, the sequentially connected air filtration system, compression system, pre-cooling system, and purification system) is connected to the supercharged side 22 of the high-temperature expander, and the supercharged side 22 of the high-temperature expander is connected
  • the supercharging side 32 of the low-temperature expander and the supercharging side 32 of the low-temperature expander are connected to the first heat exchange pipe 6 in the main heat exchanger 4, and the first heat exchange pipe 6 in the main heat exchanger 4 includes
  • the expansion side 31 of the low-temperature expander is connected to the second heat exchange pipe 7 in the main heat exchanger 4 and the rectification system 5 in two ways.
  • the rectification system extracts a stream of pressure dirty nitrogen gas from the dirty nitrogen pipe 14 and parallels it.
  • the second heat exchange pipeline 7 in the main heat exchanger 4 is connected to the expansion side 21 of the high temperature expander, and the pressure sewage nitrogen passes through the high temperature expander 2 to become low pressure sewage nitrogen.
  • the expansion side 21 of the high-temperature expander is then connected to the third heat exchange pipeline 8 in the main heat exchanger 8.
  • the outlet of the third heat exchange pipeline 8 in the main heat exchanger 4 is divided into two routes, one way is connected to the purification system Provide adsorbent regeneration gas, and the other way is connected to the pre-cooling system. That is, the low-pressure sewage nitrogen is reheated by the third heat exchange pipeline 8 in the main heat exchanger 4 to become low-pressure normal-temperature sewage nitrogen, part of which enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part is connected to the pre-cooling system to participate Prepare frozen water.
  • the low-pressure sewage nitrogen output port of the rectification system 5 is connected to the fourth heat exchange pipe 9 in the main heat exchanger 4, and the low-pressure nitrogen outlet of the rectification system 5 is connected to the fifth heat exchange pipe in the main heat exchanger 4
  • the circuit 10, the fourth heat exchange pipe 9 and the fifth heat exchange pipe 10 in the main heat exchanger 4 are jointly connected to the pre-cooling system.
  • An all-liquid air separation process based on the above-mentioned all-liquid air separation equipment is as follows: the air is filtered, compressed, pre-cooled, and purified, and then becomes compressed at a pressure of 10 to 60 bar and a temperature of 5 to 50 °C after purification. Air.
  • the purified compressed air is continuously pressurized by the supercharging side 22 of the high-temperature expander and the supercharging side 32 of the low-temperature expander, and then enters the first heat exchange pipeline 6 in the main heat exchanger 4 for heat exchange.
  • Part of the air in the first heat exchange pipeline 6 in the main heat exchanger 4 is drawn out in the middle of the main heat exchanger 4 and enters the expansion side 31 of the low-temperature expander to expand, and the other part of the air becomes high pressure at the bottom of the main heat exchanger 4 Liquid air enters the rectification system 5 after throttling.
  • the air expanded by the expansion side 31 of the low-temperature expander is divided into two paths, one path enters the second heat exchange pipe 7 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 pressurized sewage nitrogen and merges it into the second heat exchange pipe 7 in the main heat exchanger 4, and mixes and exchanges heat through the second heat exchange pipe 7 in the main heat exchanger 4
  • the waste nitrogen gas enters the expansion side 31 of the high-temperature expander and expands into low-pressure waste nitrogen gas.
  • the low-pressure waste nitrogen gas is reheated by the third heat exchange pipe 8 in the main heat exchanger 4 to become low-pressure normal-temperature waste nitrogen gas.
  • a part of the low-pressure normal temperature polluted nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part of the low-pressure normal temperature polluted nitrogen enters the pre-cooling system to participate in the production of chilled water.
  • the rectification system 5 separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon, and generates low-pressure polluted nitrogen and low-pressure nitrogen.
  • the low-pressure foul nitrogen generated by the rectification system 5 is reheated by the fourth heat exchange pipe 9 in the main heat exchanger 4, and the low-pressure nitrogen generated by the rectification system 5 is reheated by the fifth heat exchange pipe in the main heat exchanger 4.
  • Route 10 is reheated, the polluted nitrogen gas reheated by the fourth heat exchange pipe 9 in the main heat exchanger 4 and the low pressure nitrogen gas reheated by the fifth heat exchange pipe 10 in the main heat exchanger 4 Commonly connected to enter the pre-cooling system to produce chilled water.
  • the compressed air After being filtered, compressed, pre-cooled, and purified, the compressed air enters the high-temperature expander 2 and the low-temperature expander 3 for continuous pressure increase, and then enters the main heat exchanger 4 for heat exchange.
  • the air is expanded by the low-temperature expander 3.
  • the main heat exchanger 4 it is mixed and reheated with the pressure polluted nitrogen, and then enters the high temperature expander 2 to expand, and then is reheated by the main heat exchanger 4 to become low pressure and normal temperature polluted nitrogen, that is, the high temperature expander 2, the low temperature expander 3 Under high pressure and high temperature, the principle of high temperature and high enthalpy is used to perform high-efficiency expansion and refrigeration.

Abstract

The present invention relates to fully-liquefied gas separation equipment and process. The fully-liquefied gas separation equipment comprises air filtration, compression, precooling, and purification systems, a high-temperature expander, a low-temperature expander, a main heat exchanger, and a rectification system. The air filtration, compression, precooling, and purification systems are connected sequentially to a pressurizing side of the high-temperature expander, a pressurizing side of the low-temperature expander, and the main heat exchanger and then is divided into two branches, respectively connected to an expanding side of the low-temperature expander and the rectification system. The expanding side of the low-temperature expander is connected respectively to the main heat exchanger and the rectification system. The main heat exchanger in turn is connected to the expanding side of the high-temperature expander. The expanding side of the high-temperature expander in turn is connected to the main heat exchanger. The main heat exchanger in turn is connected to the purification system. A low-pressure contaminated nitrogen outlet and a low-pressure nitrogen outlet of the rectification system respectively are connected to the main heat exchanger. The heat exchanger is then connected to the precooling system. The fully-liquefied gas separation process is implemented on the basis of the fully-liquefied gas separation equipment. The present invention has a simple configuration, is easy to implement, provides high gas separation efficiency, and has a low energy consumption.

Description

全液体空分设备和工艺All-liquid air separation equipment and process 技术领域Technical field
本发明属于空分技术(从空气中分离出各种组分的技术)领域，具体涉及一种全液体空分设备以及工艺。The invention belongs to the field of air separation technology (the technology for separating various components from the air), and specifically relates to an all-liquid air separation equipment and process.
背景技术Background technique
现有的空分设备及配套工艺中，通常需要使用多台压缩机用于制冷和实现空气循环，通常还需设置冷冻设备来提供冷量，存在效率低、能耗高的不足。In the existing air separation equipment and supporting processes, multiple compressors are usually used for refrigeration and air circulation, and refrigeration equipment is usually required to provide cold capacity, which has the disadvantages of low efficiency and high energy consumption.
发明内容Summary of the invention
本发明的目的是提供一种效率较高、能耗较低的全液体空分设备。The purpose of the present invention is to provide an all-liquid air separation plant with higher efficiency and lower energy consumption.
为达到上述目的，本发明采用的技术方案是：In order to achieve the above objective, the technical solution adopted by the present invention is:
一种全液体空分设备，包括空气过滤系统、压缩系统、预冷系统、纯化系统、高温膨胀机、低温膨胀机、主换热器和用于精馏空气的精馏系统；An all-liquid air separation equipment, including an air filtration system, a compression system, a pre-cooling system, a purification system, a high-temperature expander, a low-temperature expander, a main heat exchanger, and a rectification system for rectifying air;
所述空气过滤系统、所述压缩系统、所述预冷系统、所述纯化系统依次连接后再连接至所述高温膨胀机的增压侧，所述高温膨胀机的增压侧连接所述低温膨胀机的增压侧，所述低温膨胀机的增压侧连接所述主换热器内的第一条换热管路，所述主换热器内的第一条换热管路包括与所述低温膨胀机的增压侧连接的主路、由所述主路分支出的两条支路，一条所述支路连接所述低温膨胀机的膨胀侧，另一条所述支路连接至所述精馏系统，所述低温膨胀机的膨胀侧分两路分别连接所述主换热器内的第二条换热管路、所述精馏系统，由所述精馏系统抽取一股压力污氮气的污氮气管路并入所述主换热器内的第二条换热管路，所述主换热器内的第二条换热管路连接所述高温膨胀机的膨胀侧，所述高温膨胀机的膨胀侧再连接所述主换热器内的第三条换热管路，所述主换热器内的第三条换热管路的出口分两路，一路连接所述纯化系统提供吸附剂再生气，另一路连接所述预冷系统；所述精馏系统的低压污氮气输出口连接所述主换热器内的第四条换热管路，所述精馏系统的低压氮气出口连接至所述主换热器内的第五条换热管路，所述主换热器内的第四条换热管路和第五条换热管路共同连接所述预冷系统。The air filtration system, the compression system, the pre-cooling system, and the purification system are connected in sequence and then connected to the supercharging side of the high temperature expander, and the supercharging side of the high temperature expander is connected to the low temperature The supercharging side of the expander, the supercharging side of the low-temperature expander is connected to the first heat exchange pipeline in the main heat exchanger, and the first heat exchange pipeline in the main heat exchanger includes The main circuit connected to the supercharging side of the low-temperature expander and two branch circuits branched from the main circuit, one of the branch circuits is connected to the expansion side of the low-temperature expander, and the other branch is connected to In the rectification system, the expansion side of the low-temperature expander is connected to the second heat exchange pipeline in the main heat exchanger and the rectification system in two paths, and the rectification system extracts one The sewage nitrogen pipeline of the pressure sewage nitrogen is merged into the second heat exchange pipeline in the main heat exchanger, and the second heat exchange pipeline in the main heat exchanger is connected to the expansion side of the high temperature expander , The expansion side of the high-temperature expander is then connected to the third heat exchange pipeline in the main heat exchanger, and the outlet of the third heat exchange pipeline in the main heat exchanger is divided into two ways, one way is connected The purification system provides adsorbent regeneration gas, and the other is connected to the pre-cooling system; the low-pressure sewage nitrogen output port of the rectification system is connected to the fourth heat exchange pipeline in the main heat exchanger, and the refined The low-pressure nitrogen outlet of the distillation system is connected to the 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 to the Describe the pre-cooling system.
本发明还提供上述全液体空分设备采用的全液体空分工艺，所述全液体空分工艺为：空气经过滤、压缩、预冷、纯化后，经所述高温膨胀机的增压侧和所述低温膨胀机的增压侧连续增压后，进入所述主换热器内的第一条换热管路换热，所述主换热器内的第一条换热管路内的一部分空气在所述主换热器的中部被抽出并进入所述低温膨胀机的膨胀端膨胀，另一部分空气在所述主换热器的底部成为高压液空并进入所述精馏系统；经所述低温膨胀机的膨胀 端膨胀后的空气分两路分别进入所述主换热器内的第二条换热管路换热和所述精馏系统精馏；所述精馏系统抽取一股压力污氮气并入所述主换热器内的第二条换热管路，经所述主换热器内的第二条换热管路混合、换热后的污氮气再进入所述高温膨胀机的膨胀端膨胀成为低压污氮气，所述低压污氮气经所述主换热器内的第三条换热管路复热成为低压常温污氮气；一部分所述低压常温污氮气进入所述纯化系统而为所述纯化系统提供吸附剂再生气，另一部分所述低压常温污氮气进入所述预冷系统；所述精馏系统产生的低压污氮气经所述主换热器内的第四条换热管路复热，所述精馏系统产生的低压氮气经所述主换热器内的第五条换热管路复热，经所述主换热器内的第四条换热管路复热后的污氮气和经所述主换热器内的第五条换热管路复热后的氮气共同连接进入所述预冷系统。The present invention also provides an all-liquid air separation process adopted by the above-mentioned all-liquid air separation equipment. The all-liquid air separation process is as follows: after air is filtered, compressed, pre-cooled, and purified, it passes through the pressurizing side of the high-temperature expander and After the pressurization side of the low-temperature expander is continuously pressurized, it enters the first heat exchange pipeline in the main heat exchanger to exchange heat, and the heat exchange in the first heat exchange pipeline in the main heat exchanger Part of the air is drawn out in the middle of the main heat exchanger and enters the expansion end of the low-temperature expander to expand, and another part of the air becomes high-pressure liquid at the bottom of the main heat exchanger and enters the rectification system; The air expanded at the expansion end of the cryogenic expander enters the second heat exchange pipe in the main heat exchanger in two ways for heat exchange and rectification by the rectification system; the rectification system draws one The pressurized sewage nitrogen is merged into the second heat exchange pipeline in the main heat exchanger, and the mixed and heat exchanged sewage nitrogen enters the second heat exchange pipeline in the main heat exchanger. The expansion end of the high-temperature expander expands into low-pressure sewage nitrogen, and the low-pressure sewage nitrogen is reheated by the third heat exchange pipe in the main heat exchanger to become low-pressure normal-temperature sewage nitrogen; part of the low-pressure normal-temperature sewage nitrogen enters the plant The purification system provides adsorbent regeneration gas for the purification system, and another part of the low-pressure normal temperature polluted nitrogen enters the pre-cooling system; the low-pressure polluted nitrogen generated by the rectification system passes through the second in the main heat exchanger Four heat exchange pipes are reheated. The low-pressure nitrogen generated by the rectification system is reheated by the fifth heat exchange pipe in the main heat exchanger, and is exchanged by the fourth heat exchange pipe in the main heat exchanger. The reheated waste nitrogen gas of the heat pipe and the reheated nitrogen gas of the fifth heat exchange pipe in the main heat exchanger are connected together to enter the pre-cooling system.
优选的，空气经过滤、压缩、预冷、纯化脱除水和二氧化碳后变成压力为10～60bar，温度为5～50℃纯化后的压缩空气。Preferably, the air is filtered, compressed, pre-cooled, purified to remove water and carbon dioxide into compressed air with a pressure of 10-60 bar and a temperature of 5-50°C.
优选的，空气进入所述中压纯化系统脱除水和二氧化碳。Preferably, air enters the medium pressure purification system to remove water and carbon dioxide.
优选的，所述高压液空经节流后进入所述精馏系统。Preferably, the high-pressure liquid air enters the rectification system after throttling.
优选的，所述精馏系统分离、液化得到液氮、液氧和液氩。Preferably, the rectification system separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon.
由于上述技术方案运用，本发明与现有技术相比具有下列优点：本发明配置简单、便于实施，且空分效率较高，氧提取率高，而能耗较低。Due to the application of the above technical solutions, the present invention has the following advantages compared with the prior art: the present invention is simple in configuration, easy to implement, and has high air separation efficiency, high oxygen extraction rate, and low energy consumption.
附图说明Description of the drawings
附图1为本发明的全液体空分设备的工艺流程图。Figure 1 is a process flow diagram of the all-liquid air separation plant of the present invention.
以上附图中：1、过滤、压缩、预冷、纯化系统(包括空气过滤系统、压缩系统、预冷系统、纯化系统)；2、高温膨胀机；21、高温膨胀机的膨胀侧；22、高温膨胀机的增压侧；3、低温膨胀机；31、低温膨胀机的膨胀侧；32、低温膨胀机的增压侧；4、主换热器；5、精馏系统；6、第一条换热管路；7、第二条换热管路；8、第三条换热管路；9、第四条换热管路；10、第五条换热管路；11、主路；12、支路；13、支路；14、污氮气管路。In the above drawings: 1. Filtration, compression, pre-cooling, purification system (including air filtration system, compression system, pre-cooling system, purification system); 2. High temperature expander; 21, expansion side of high temperature expander; 22, The supercharging side of the high temperature expander; 3. The low temperature expander; 31. The expansion side of the low temperature expander; 32. The supercharging side of the low temperature expander; 4. The main heat exchanger; 5. The rectification system; 6. The first 7. The second heat exchange pipeline; 8. The third heat exchange pipeline; 9. The fourth heat exchange pipeline; 10. The fifth heat exchange pipeline; 11. Main circuit ; 12, branch; 13, branch; 14, sewage nitrogen pipeline.
具体实施方式Detailed ways
下面结合附图所示的实施例对本发明作进一步描述。The present invention will be further described below in conjunction with the embodiments shown in the drawings.
实施例一：如附图1所示，一种全液体空分设备，包括空气过滤、压缩、预冷、纯化系统1以及高温膨胀机2、低温膨胀机3、主换热器4、用于精馏空气的精馏系统5。膨胀机，包括高温膨胀机2、低温膨胀机3，均具有用于膨胀气体使其降压的膨胀侧和用于压缩气体使其增压的增压侧，即高温膨胀机2具有高温膨胀机的膨胀侧21和高温膨胀机的增压侧22，低温膨胀机3具有低温膨胀机的膨胀侧31和低温膨胀机的增压侧32。Embodiment 1: As shown in Figure 1, an all-liquid air separation plant includes air filtration, compression, pre-cooling, purification system 1, high temperature expander 2, low temperature expander 3, main heat exchanger 4, and Distillation system for rectifying air5. The expanders, including the high-temperature expander 2 and the low-temperature expander 3, each have an expansion side for expanding the gas to depressurize it and a supercharging side for compressing the gas to pressurize it, that is, the high-temperature expander 2 has a high-temperature expander The expansion side 21 and the supercharging side 22 of the high temperature expander, the low temperature expander 3 has the expansion side 31 of the low temperature expander and the supercharging side 32 of the low temperature expander.
空气过滤、压缩、预冷、纯化系统1(即依次连接的空气过滤系统、压缩系统、预冷系 统、纯化系统)连接至高温膨胀机的增压侧22，高温膨胀机的增压侧22连接低温膨胀机的增压侧32，低温膨胀机的增压侧32连接主换热器4内的第一条换热管路6，主换热器4内的第一条换热管路6包括与低温膨胀机的增压侧32连接的主路11、由主路11分支出的两条支路12、13，一条支路12连接低温膨胀机的膨胀侧31，另一条支路13连接至精馏系统5。低温膨胀机的膨胀侧31分两路分别连接主换热器4内的第二条换热管路7、精馏系统5，由精馏系统抽取一股压力污氮气的污氮气管路14并入主换热器4内的第二条换热管路6。主换热器4内的第二条换热管路7连接高温膨胀机的膨胀侧21，压力污氮气经高温膨胀机2成为低压污氮气。高温膨胀机的膨胀侧21再连接主换热器8内的第三条换热管路8，主换热器4内的第三条换热管路8的出口分两路，一路连接纯化系统提供吸附剂再生气，另一路连接预冷系统。即低压污氮气经主换热器4内的第三条换热管路8复热成为低压常温污氮气，一部分进入纯化系统，为纯化系统提供吸附剂再生气，另一部分连接预冷系统，参与制取冷冻水。精馏系统5的低压污氮气输出口连接主换热器4内的第四条换热管路9，精馏系统5的低压氮气出口连接至主换热器4内的第五条换热管路10，主换热器4内的第四条换热管路9和第五条换热管路10共同连接预冷系统。The air filtration, compression, pre-cooling, and purification system 1 (that is, the sequentially connected air filtration system, compression system, pre-cooling system, and purification system) is connected to the supercharged side 22 of the high-temperature expander, and the supercharged side 22 of the high-temperature expander is connected The supercharging side 32 of the low-temperature expander and the supercharging side 32 of the low-temperature expander are connected to the first heat exchange pipe 6 in the main heat exchanger 4, and the first heat exchange pipe 6 in the main heat exchanger 4 includes The main road 11 connected to the supercharging side 32 of the low-temperature expander, two branch roads 12 and 13 branched from the main road 11, one branch road 12 is connected to the expansion side 31 of the low-temperature expander, and the other branch road 13 is connected to Distillation system 5. The expansion side 31 of the low-temperature expander is connected to the second heat exchange pipe 7 in the main heat exchanger 4 and the rectification system 5 in two ways. The rectification system extracts a stream of pressure dirty nitrogen gas from the dirty nitrogen pipe 14 and parallels it. Into the second heat exchange pipeline 6 in the main heat exchanger 4. The second heat exchange pipeline 7 in the main heat exchanger 4 is connected to the expansion side 21 of the high temperature expander, and the pressure sewage nitrogen passes through the high temperature expander 2 to become low pressure sewage nitrogen. The expansion side 21 of the high-temperature expander is then connected to the third heat exchange pipeline 8 in the main heat exchanger 8. The outlet of the third heat exchange pipeline 8 in the main heat exchanger 4 is divided into two routes, one way is connected to the purification system Provide adsorbent regeneration gas, and the other way is connected to the pre-cooling system. That is, the low-pressure sewage nitrogen is reheated by the third heat exchange pipeline 8 in the main heat exchanger 4 to become low-pressure normal-temperature sewage nitrogen, part of which enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part is connected to the pre-cooling system to participate Prepare frozen water. The low-pressure sewage nitrogen output port of the rectification system 5 is connected to the fourth heat exchange pipe 9 in the main heat exchanger 4, and the low-pressure nitrogen outlet of the rectification system 5 is connected to the fifth heat exchange pipe in the main heat exchanger 4 The circuit 10, the fourth heat exchange pipe 9 and the fifth heat exchange pipe 10 in the main heat exchanger 4 are jointly connected to the pre-cooling system.
基于上述的全液体空分设备而实现的一种全液体空分工艺为：空气经过滤、压缩、预冷、纯化后，变成压力为10～60bar，温度为5～50℃纯化后的压缩空气。纯化后的压缩空气经高温膨胀机的增压侧22和低温膨胀机的增压侧32连续增压后，进入主换热器4内的第一条换热管路6换热，主换热器4内的第一条换热管路6内的一部分空气在主换热器4的中部被抽出并进入低温膨胀机的膨胀侧31膨胀，另一部分空气在主换热器4的底部成为高压液空，经节流后进入精馏系统5。经低温膨胀机的膨胀侧31膨胀后的空气分两路，一路进入主换热器4内的第二条换热管路7换热，另一路进入精馏系统5精馏。精馏系统5抽取一股压力污氮气，并入主换热器4内的第二条换热管路7，经主换热器4内的第二条换热管路7混合、换热后的污氮气再进入高温膨胀机的膨胀侧31膨胀成为低压污氮气，低压污氮气经主换热器4内的第三条换热管路8复热成为低压常温污氮气。一部分低压常温污氮气进入纯化系统，为纯化系统提供吸附剂再生气，另一部分低压常温污氮气进入预冷系统，参与制取冷冻水。精馏系统5分离、液化得到液氮、液氧和液氩，并产生低压污氮气和低压氮气。精馏系统5产生的低压污氮气经主换热器4内的第四条换热管路9复热，精馏系统5产生的低压氮气经主换热器4内的第五条换热管路10复热，经主换热器4内的第四条换热管路9复热后的污氮气和经主换热器4内的第五条换热管路10复热后的低压氮气共同连接进入预冷系统制取冷冻水。An all-liquid air separation process based on the above-mentioned all-liquid air separation equipment is as follows: the air is filtered, compressed, pre-cooled, and purified, and then becomes compressed at a pressure of 10 to 60 bar and a temperature of 5 to 50 ℃ after purification. Air. The purified compressed air is continuously pressurized by the supercharging side 22 of the high-temperature expander and the supercharging side 32 of the low-temperature expander, and then enters the first heat exchange pipeline 6 in the main heat exchanger 4 for heat exchange. Part of the air in the first heat exchange pipeline 6 in the main heat exchanger 4 is drawn out in the middle of the main heat exchanger 4 and enters the expansion side 31 of the low-temperature expander to expand, and the other part of the air becomes high pressure at the bottom of the main heat exchanger 4 Liquid air enters the rectification system 5 after throttling. The air expanded by the expansion side 31 of the low-temperature expander is divided into two paths, one path enters the second heat exchange pipe 7 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 pressurized sewage nitrogen and merges it into the second heat exchange pipe 7 in the main heat exchanger 4, and mixes and exchanges heat through the second heat exchange pipe 7 in the main heat exchanger 4 The waste nitrogen gas enters the expansion side 31 of the high-temperature expander and expands into low-pressure waste nitrogen gas. The low-pressure waste nitrogen gas is reheated by the third heat exchange pipe 8 in the main heat exchanger 4 to become low-pressure normal-temperature waste nitrogen gas. A part of the low-pressure normal temperature polluted nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and the other part of the low-pressure normal temperature polluted nitrogen enters the pre-cooling system to participate in the production of chilled water. The rectification system 5 separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon, and generates low-pressure polluted nitrogen and low-pressure nitrogen. The low-pressure foul nitrogen generated by the rectification system 5 is reheated by the fourth heat exchange pipe 9 in the main heat exchanger 4, and the low-pressure nitrogen generated by the rectification system 5 is reheated by the fifth heat exchange pipe in the main heat exchanger 4. Route 10 is reheated, the polluted nitrogen gas reheated by the fourth heat exchange pipe 9 in the main heat exchanger 4 and the low pressure nitrogen gas reheated by the fifth heat exchange pipe 10 in the main heat exchanger 4 Commonly connected to enter the pre-cooling system to produce chilled water.
上述方案中：In the above scheme:
经过滤、压缩、预冷、纯化后的压缩空气进入高温膨胀机2、低温膨胀机3的增压侧连 续增压，然后进主换热器4换热后，空气经低温膨胀机3膨胀、在主换热器4内与压力污氮混合复热后进入高温膨胀机2膨胀、再经主换热器4复热，变成低压常温污氮气，即高温膨胀机2、低温膨胀机3在高压、温度较高情况下，利用高温高焓值原理，进行高效率膨胀制冷。After being filtered, compressed, pre-cooled, and purified, the compressed air enters the high-temperature expander 2 and the low-temperature expander 3 for continuous pressure increase, and then enters the main heat exchanger 4 for heat exchange. The air is expanded by the low-temperature expander 3. In the main heat exchanger 4, it is mixed and reheated with the pressure polluted nitrogen, and then enters the high temperature expander 2 to expand, and then is reheated by the main heat exchanger 4 to become low pressure and normal temperature polluted nitrogen, that is, the high temperature expander 2, the low temperature expander 3 Under high pressure and high temperature, the principle of high temperature and high enthalpy is used to perform high-efficiency expansion and refrigeration.
上述实施例只为说明本发明的技术构思及特点，其目的在于让熟悉此项技术的人士能够了解本发明的内容并据以实施，并不能以此限制本发明的保护范围。凡根据本发明精神实质所作的等效变化或修饰，都应涵盖在本发明的保护范围之内。The above-mentioned embodiments are only to illustrate the technical concept and characteristics of the present invention, and their purpose is to enable those familiar with the technology to understand the content of the present invention and implement them accordingly, and cannot limit the protection scope of the present invention. All equivalent changes or modifications made according to the spirit of the present invention should be covered by the protection scope of the present invention.

Claims (6)

  1. 一种全液体空分设备，其特征在于：所述全液体空分设备包括空气过滤系统、压缩系统、预冷系统、纯化系统、高温膨胀机、低温膨胀机、主换热器和用于精馏空气的精馏系统；An all-liquid air separation equipment, characterized in that: the all-liquid air separation equipment includes an air filter system, a compression system, a pre-cooling system, a purification system, a high-temperature expander, a low-temperature expander, a main heat exchanger, and a Distillation system for distilling air;
    所述空气过滤系统、所述压缩系统、所述预冷系统、所述纯化系统依次连接后再连接至所述高温膨胀机的增压侧，所述高温膨胀机的增压侧连接所述低温膨胀机的增压侧，所述低温膨胀机的增压侧连接所述主换热器内的第一条换热管路，所述主换热器内的第一条换热管路包括与所述低温膨胀机的增压侧连接的主路、由所述主路分支出的两条支路，一条所述支路连接所述低温膨胀机的膨胀侧，另一条所述支路连接至所述精馏系统，所述低温膨胀机的膨胀侧分两路分别连接所述主换热器内的第二条换热管路、所述精馏系统，由所述精馏系统抽取一股压力污氮气的污氮气管路并入所述主换热器内的第二条换热管路，所述主换热器内的第二条换热管路连接所述高温膨胀机的膨胀侧，所述高温膨胀机的膨胀侧再连接所述主换热器内的第三条换热管路，所述主换热器内的第三条换热管路的出口分两路，一路连接所述纯化系统提供吸附剂再生气，另一路连接所述预冷系统；所述精馏系统的低压污氮气输出口连接所述主换热器内的第四条换热管路，所述精馏系统的低压氮气出口连接至所述主换热器内的第五条换热管路，所述主换热器内的第四条换热管路和第五条换热管路共同连接所述预冷系统。The air filtration system, the compression system, the pre-cooling system, and the purification system are connected in sequence and then connected to the supercharging side of the high temperature expander, and the supercharging side of the high temperature expander is connected to the low temperature The supercharging side of the expander, the supercharging side of the low-temperature expander is connected to the first heat exchange pipeline in the main heat exchanger, and the first heat exchange pipeline in the main heat exchanger includes The main circuit connected to the supercharging side of the low-temperature expander and two branch circuits branched from the main circuit, one of the branch circuits is connected to the expansion side of the low-temperature expander, and the other branch is connected to In the rectification system, the expansion side of the low-temperature expander is connected to the second heat exchange pipeline in the main heat exchanger and the rectification system in two ways, and the rectification system extracts one The sewage nitrogen pipeline of the pressure sewage nitrogen is merged into the second heat exchange pipeline in the main heat exchanger, and the second heat exchange pipeline in the main heat exchanger is connected to the expansion side of the high temperature expander , The expansion side of the high-temperature expander is then connected to the third heat exchange pipeline in the main heat exchanger, and the outlet of the third heat exchange pipeline in the main heat exchanger is divided into two ways, one way is connected The purification system provides adsorbent regeneration gas, and the other is connected to the pre-cooling system; the low-pressure sewage nitrogen output port of the rectification system is connected to the fourth heat exchange pipeline in the main heat exchanger, and the refined The low-pressure nitrogen outlet of the distillation system is connected to the 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 to the Describe the pre-cooling system.
  2. 一种全液体空分工艺，基于如权利要求1所述的全液体空分设备而实现，其特征在于：所述全液体空分工艺为：空气经过滤、压缩、预冷、纯化脱除水和二氧化碳后变成压力为10～60bar，温度为5～50℃纯化后的压缩空气，所述纯化后的压缩空气经所述高温膨胀机的增压侧和所述低温膨胀机的增压侧连续增压后，进入所述主换热器内的第一条换热管路换热，所述主换热器内的第一条换热管路内的一部分空气在所述主换热器的中部被抽出并进入所述低温膨胀机的膨胀端膨胀，另一部分空气在所述主换热器的底部成为高压液空并经节流后进入所述精馏系统；经所述低温膨胀机的膨胀端膨胀后的空气分两路分别进入所述主换热器内的第二条换热管路换热和所述精馏系统精馏；所述精馏系统抽取一股压力污氮气并入所述主换热器内的第二条换热管路，经所述主换热器内的第二条换热管路混合、换热后的污氮气再进入所述高温膨胀机的膨胀端膨胀成为低压污氮气，所述低压污氮气经所述主换热器内的第三条换热管路复热成为低压常温污氮气；一部分所述低压常温污氮气进入所述纯化系统而为所述纯化系统提供吸附剂再生气，另一部分所述低压常温污氮气进入所述预冷系统参与制取冷冻水；所述精馏系统分离、液化得到液氮、液氧和液氩；所述精馏系统产生的低压污氮气经所述主换热器内的第四条换热管路复热，所述精馏系统产生的低压氮气经所述主换热器内的第五条换热管路复热，经所述主换热器内的第四条换热管路复热后的污氮气和经所述主换热器内的第五条换热管路复热后的氮气共同连接进入所述预冷系统制取冷冻水。An all-liquid air separation process, based on the all-liquid air separation equipment as claimed in claim 1, is characterized in that: the all-liquid air separation process is: air is filtered, compressed, pre-cooled, purified to remove water With carbon dioxide, it becomes purified compressed air with a pressure of 10-60 bar and a temperature of 5-50°C. The purified compressed air passes through the supercharging side of the high-temperature expander and the supercharging side of the low-temperature expander After continuous pressurization, it enters the first heat exchange pipeline in the main heat exchanger to exchange heat, and part of the air in the first heat exchange pipeline in the main heat exchanger is in the main heat exchanger The middle part of the air is drawn out and enters the expansion end of the low-temperature expander to expand, and the other part of the air becomes high-pressure liquid at the bottom of the main heat exchanger and enters the rectification system after being throttled; through the low-temperature expander The expanded air at the expansion end of the expansion end enters the second heat exchange pipe in the main heat exchanger in two ways for heat exchange and rectification by the rectification system; the rectification system extracts a stream of pressure dirty nitrogen gas and The second heat exchange pipeline into the main heat exchanger is mixed and heat exchanged by the second heat exchange pipeline in the main heat exchanger, and then enters the high-temperature expander for expansion. The end expansion becomes low-pressure sewage nitrogen, and the low-pressure sewage nitrogen is reheated by the third heat exchange pipe in the main heat exchanger to become low-pressure normal-temperature sewage nitrogen; a part of the low-pressure normal-temperature sewage nitrogen enters the purification system for the purpose of The purification system provides adsorbent regeneration gas, and another part of the low-pressure normal temperature polluted nitrogen enters the pre-cooling system to participate in the production of chilled water; the rectification system separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon; The low-pressure foul nitrogen generated by the rectification system is reheated by the fourth heat exchange pipe in the main heat exchanger, and the low-pressure nitrogen generated by the rectification system is reheated by the fifth heat exchange pipe in the main heat exchanger. The pipeline is reheated, the waste nitrogen after being reheated by the fourth heat exchange pipe in the main heat exchanger and the nitrogen after being reheated by the fifth heat exchange pipe in the main heat exchanger are shared Connect to the pre-cooling system to produce chilled water.
  3. 一种全液体空分工艺，基于如权利要求1所述的全液体空分设备而实现，其特征在于：所述全液体空分工艺为：空气经过滤、压缩、预冷、纯化后，经所述高温膨胀机的增压侧和所述低温膨胀机的增压侧连续增压后，进入所述主换热器内的第一条换热管路换热，所述主换热器内的第一条换热管路内的一部分空气在所述主换热器的中部被抽出并进入所述低温膨胀机的膨胀端膨胀，另一部分空气在所述主换热器的底部成为高压液空并进入所述精馏系统；经所述低温膨胀机的膨胀端膨胀后的空气分两路分别进入所述主换热器内的第二条换热管路换热和所述精馏系统精馏；所述精馏系统抽取一股压力污氮气并入所述主换热器内的第二条换热管路，经所述主换热器内的第二条换热管路混合、换热后的污氮气再进入所述高温膨胀机的膨胀端膨胀成为低压污氮气，所述低压污氮气经所述主换热器内的第三条换热管路复热成为低压常温污氮气；一部分所述低压常温污氮气进入所述纯化系统而为所述纯化系统提供吸附剂再生气，另一部分所述低压常温污氮气进入所述预冷系统；所述精馏系统产生的低压污氮气经所述主换热器内的第四条换热管路复热，所述精馏系统产生的低压氮气经所述主换热器内的第五条换热管路复热，经所述主换热器内的第四条换热管路复热后的污氮气和经所述主换热器内的第五条换热管路复热后的氮气共同连接进入所述预冷系统。An all-liquid air separation process, which is realized based on the all-liquid air separation equipment as claimed in claim 1, is characterized in that: the all-liquid air separation process is: air is filtered, compressed, pre-cooled, purified, and passed After the supercharging side of the high-temperature expander and the supercharging side of the low-temperature expander are continuously pressurized, they enter the first heat exchange pipeline in the main heat exchanger to exchange heat. A part of the air in the first heat exchange pipeline is drawn out in the middle of the main heat exchanger and enters the expansion end of the low-temperature expander to expand, and the other part of the air becomes a high-pressure liquid at the bottom of the main heat exchanger The air enters the rectification system; the air expanded by the expansion end of the low-temperature expander enters the second heat exchange pipeline in the main heat exchanger in two ways for heat exchange and the rectification system Rectification; the rectification system extracts a stream of pressure dirty nitrogen gas and merges it into the second heat exchange pipeline in the main heat exchanger, and mixes it through the second heat exchange pipeline in the main heat exchanger, The heat-exchanged sewage nitrogen enters the expansion end of the high-temperature expander and expands into low-pressure sewage nitrogen. The low-pressure sewage nitrogen is reheated by the third heat exchange pipe in the main heat exchanger to become low-pressure normal-temperature sewage nitrogen. A part of the low-pressure normal temperature polluted nitrogen enters the purification system to provide adsorbent regeneration gas for the purification system, and another part of the low-pressure normal temperature polluted nitrogen enters the pre-cooling system; the low-pressure polluted nitrogen generated by the rectification system It is reheated through the fourth heat exchange pipe in the main heat exchanger, and the low-pressure nitrogen generated by the rectification system is reheated through the fifth heat exchange pipe in the main heat exchanger. The contaminated nitrogen gas reheated by the fourth heat exchange pipe in the main heat exchanger and the nitrogen gas reheated by the fifth heat exchange pipe in the main heat exchanger are connected together to enter the pre-cooling system.
  4. 根据权利要求3所述的全液体空分工艺，其特征在于：空气经过滤、压缩、预冷、纯化脱除水和二氧化碳后变成压力为10～60bar，温度为5～50℃纯化后的压缩空气。The all-liquid air separation process according to claim 3, characterized in that: the air is filtered, compressed, pre-cooled, purified to remove water and carbon dioxide into a pressure of 10 to 60 bar, and a temperature of 5 to 50 ℃ after purification. Compressed air.
  5. 根据权利要求3所述的全液体空分工艺，其特征在于：所述高压液空经节流后进入所述精馏系统。The all-liquid air separation process according to claim 3, wherein the high-pressure liquid air enters the rectification system after throttling.
  6. 根据权利要求3所述的全液体空分工艺，其特征在于：所述精馏系统分离、液化得到液氮、液氧和液氩。The all-liquid air separation process according to claim 3, wherein the rectification system separates and liquefies to obtain liquid nitrogen, liquid oxygen and liquid argon.
PCT/CN2021/079018 2020-03-11 2021-03-04 Fully-liquefied gas separation equipment and process WO2021179980A1 (en)

Priority Applications (1)

Application Number Priority Date Filing Date Title
US17/930,489 US20230003445A1 (en) 2020-03-11 2022-09-08 Full liquid-product air separation equipment and process therefor

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
CN202010165585.8A CN111322832A (en) 2020-03-11 2020-03-11 Full liquid air separation plant and process
CN202010165585.8 2020-03-11

Related Child Applications (1)

Application Number Title Priority Date Filing Date
US17/930,489 Continuation US20230003445A1 (en) 2020-03-11 2022-09-08 Full liquid-product air separation equipment and process therefor

Publications (1)

Publication Number Publication Date
WO2021179980A1 true WO2021179980A1 (en) 2021-09-16

Family

ID=71165546

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/CN2021/079018 WO2021179980A1 (en) 2020-03-11 2021-03-04 Fully-liquefied gas separation equipment and process

Country Status (3)

Country Link
US (1) US20230003445A1 (en)
CN (1) CN111322832A (en)
WO (1) WO2021179980A1 (en)

Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113758151A (en) * 2021-10-09 2021-12-07 乔治洛德方法研究和开发液化空气有限公司 Method for the cryogenic separation of air and air separation plant
WO2023213955A2 (en) 2022-05-05 2023-11-09 Thomas Leiber Driving dynamics system, vehicle and method for operating a driving dynamics system

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN111322832A (en) * 2020-03-11 2020-06-23 苏州市兴鲁空分设备科技发展有限公司 Full liquid air separation plant and process
CN114111218A (en) * 2020-08-25 2022-03-01 贵州盈德气体有限公司 Novel energy-saving process for air separation liquefaction of compressed air

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH09264666A (en) * 1996-03-29 1997-10-07 Taiyo Toyo Sanso Co Ltd Nitrogen and oxygen manufacturing system
CN108286870A (en) * 2018-02-24 2018-07-17 杭州福斯达深冷装备股份有限公司 A kind of method that cryogenic rectification produces liquid
CN109405414A (en) * 2018-11-27 2019-03-01 薛鲁 Liquid space division device
CN110207457A (en) * 2019-06-08 2019-09-06 苏州制氧机股份有限公司 It is a kind of can liquid nitrogen processed air separation plant and its application method
CN111322832A (en) * 2020-03-11 2020-06-23 苏州市兴鲁空分设备科技发展有限公司 Full liquid air separation plant and process
CN211926303U (en) * 2020-03-11 2020-11-13 苏州市兴鲁空分设备科技发展有限公司 Full liquid air separation plant

Family Cites Families (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102141337B (en) * 2011-03-30 2013-05-01 苏州市兴鲁空分设备科技发展有限公司 Method for separating air
CN104061756B (en) * 2014-06-09 2016-02-17 杭州杭氧股份有限公司 Returning polluted nitrogen gas demi-inflation refrigeration and partial boost enter pressure column and to be coupled the method and device of producing nitrogen under pressure product
US10295252B2 (en) * 2015-10-27 2019-05-21 Praxair Technology, Inc. System and method for providing refrigeration to a cryogenic separation unit
CN108731379A (en) * 2018-07-24 2018-11-02 杭州杭氧股份有限公司 A kind of amount of liquid is adjustable and produces the air separation plant and production method of more specification oxygen products simultaneously
CN209085172U (en) * 2018-07-24 2019-07-09 杭州杭氧股份有限公司 A kind of amount of liquid is adjustable and produces the air separation plant of more specification oxygen products simultaneously
CN109838975B (en) * 2019-03-22 2024-01-16 杭州特盈能源技术发展有限公司 Low-energy-consumption liquid nitrogen preparation device and process

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH09264666A (en) * 1996-03-29 1997-10-07 Taiyo Toyo Sanso Co Ltd Nitrogen and oxygen manufacturing system
CN108286870A (en) * 2018-02-24 2018-07-17 杭州福斯达深冷装备股份有限公司 A kind of method that cryogenic rectification produces liquid
CN109405414A (en) * 2018-11-27 2019-03-01 薛鲁 Liquid space division device
CN110207457A (en) * 2019-06-08 2019-09-06 苏州制氧机股份有限公司 It is a kind of can liquid nitrogen processed air separation plant and its application method
CN111322832A (en) * 2020-03-11 2020-06-23 苏州市兴鲁空分设备科技发展有限公司 Full liquid air separation plant and process
CN211926303U (en) * 2020-03-11 2020-11-13 苏州市兴鲁空分设备科技发展有限公司 Full liquid air separation plant

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN113758151A (en) * 2021-10-09 2021-12-07 乔治洛德方法研究和开发液化空气有限公司 Method for the cryogenic separation of air and air separation plant
CN113758151B (en) * 2021-10-09 2022-10-21 乔治洛德方法研究和开发液化空气有限公司 Method for the cryogenic separation of air and air separation plant
WO2023213955A2 (en) 2022-05-05 2023-11-09 Thomas Leiber Driving dynamics system, vehicle and method for operating a driving dynamics system

Also Published As

Publication number Publication date
US20230003445A1 (en) 2023-01-05
CN111322832A (en) 2020-06-23

Similar Documents

Publication Publication Date Title
WO2021179980A1 (en) Fully-liquefied gas separation equipment and process
CN109838975B (en) Low-energy-consumption liquid nitrogen preparation device and process
CN110701870B (en) Air separation device and method utilizing LNG cold energy
US7469556B2 (en) Natural gas liquefaction system
CN211926303U (en) Full liquid air separation plant
JP2009529648A (en) Cryogenic air separation method and apparatus
CN110207457B (en) Air separation equipment capable of preparing liquid nitrogen and application method thereof
CN108061428A (en) A kind of purity nitrogen device for making and technique
KR20200088399A (en) Cryogenic distillation method and apparatus for producing pressurized air by an expander booster connected to a nitrogen expander for braking
CN102721263A (en) System and method for separating air by utilizing cryogenic cooling technology
CN108286870A (en) A kind of method that cryogenic rectification produces liquid
CN104390427B (en) High-temperature and low-temperature expansion energy-saving nitrogen production device and nitrogen production method
US3233418A (en) Apparatus for liquefying helium
CN209085172U (en) A kind of amount of liquid is adjustable and produces the air separation plant of more specification oxygen products simultaneously
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
WO2019127180A1 (en) Cryogenic rectification process-based method for producing air product, and air separation system
CN213578367U (en) Device for producing oxygen and nitrogen by separating air through cryogenic rectification
US20180142950A1 (en) Lng integration with cryogenic unit
CN216790655U (en) Low-energy-consumption device for preparing pure nitrogen in single tower
CN211316726U (en) Air separation plant with double-pump internal pressure and synergistic tower
CN103438663A (en) Device and process for preparing high-purity oxygen and nitrogen under ultra-low pressure
CN114165987A (en) Liquid carbon dioxide production device and production method thereof
CN109357475B (en) System for cascade utilization LNG cold energy prepares liquid oxygen liquid nitrogen
RU2678236C1 (en) Method of liquefaction of natural gas through cycle of partial liquefaction due to change in pressure and installation for its implementation

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 21768446

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 21768446

Country of ref document: EP

Kind code of ref document: A1