WO2021179980A1 - 全液体空分设备和工艺 - Google Patents
全液体空分设备和工艺 Download PDFInfo
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- 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
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- heat exchanger
- low
- heat exchange
- main heat
- pressure
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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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—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
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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
- F25J3/04248—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
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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
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—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
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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
- 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
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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
- 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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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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
- 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
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
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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
- 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
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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
- F25J3/04642—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
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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
- F25J3/04642—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
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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
- F25J3/04642—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.
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- Engineering & Computer Science (AREA)
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- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
本发明涉及一种全液体空分设备和工艺,全液体空分设备包括空气过滤、压缩、预冷、纯化***以及高温膨胀机、低温膨胀机、主换热器、精馏***。空气过滤、压缩、预冷、纯化***依次连接高温膨胀机的增压侧、低温膨胀机的增压侧、主换热器后分为两条支路,分别连接低温膨胀机的膨胀侧、精馏***,低温膨胀机的膨胀侧分两路分别连接主换热器、精馏***,主换热器再连接高温膨胀机的膨胀侧,高温膨胀机的膨胀侧再连接主换热器,主换热器再连接纯化***,精馏***的低压污氮气输出口、低压氮气出口分别连接主换热器,主换热器再连接预冷***。全液体空分工艺基于该全液体空分设备实现。本发明配置简单、便于实施,空分效率高,能耗低。
Description
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。
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。
发明内容
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。
为达到上述目的,本发明采用的技术方案是:
一种全液体空分设备,包括空气过滤***、压缩***、预冷***、纯化***、高温膨胀机、低温膨胀机、主换热器和用于精馏空气的精馏***;
所述空气过滤***、所述压缩***、所述预冷***、所述纯化***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***,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***,由所述精馏***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***提供吸附剂再生气,另一路连接所述预冷***;所述精馏***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***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***。
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***;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***精馏;所述精馏***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***而为所述纯化***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***;所述精馏***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***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***。
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。
优选的,空气进入所述中压纯化***脱除水和二氧化碳。
优选的,所述高压液空经节流后进入所述精馏***。
优选的,所述精馏***分离、液化得到液氮、液氧和液氩。
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。
附图1为本发明的全液体空分设备的工艺流程图。
以上附图中:1、过滤、压缩、预冷、纯化***(包括空气过滤***、压缩***、预冷***、纯化***);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***;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。
下面结合附图所示的实施例对本发明作进一步描述。
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***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***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。
空气过滤、压缩、预冷、纯化***1(即依次连接的空气过滤***、压缩***、预冷系 统、纯化***)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***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***5,由精馏***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***提供吸附剂再生气,另一路连接预冷***。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***,为纯化***提供吸附剂再生气,另一部分连接预冷***,参与制取冷冻水。精馏***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***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***。
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***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***5精馏。精馏***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***,为纯化***提供吸附剂再生气,另一部分低压常温污氮气进入预冷***,参与制取冷冻水。精馏***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***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***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***制取冷冻水。
上述方案中:
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。
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。
Claims (6)
- 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***、压缩***、预冷***、纯化***、高温膨胀机、低温膨胀机、主换热器和用于精馏空气的精馏***;所述空气过滤***、所述压缩***、所述预冷***、所述纯化***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***,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***,由所述精馏***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***提供吸附剂再生气,另一路连接所述预冷***;所述精馏***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***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***。
- 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***;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***精馏;所述精馏***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***而为所述纯化***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***参与制取冷冻水;所述精馏***分离、液化得到液氮、液氧和液氩;所述精馏***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***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***制取冷冻水。
- 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***;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***精馏;所述精馏***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***而为所述纯化***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***;所述精馏***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***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***。
- 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。
- 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***。
- 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***分离、液化得到液氮、液氧和液氩。
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WO2023213955A2 (de) | 2022-05-05 | 2023-11-09 | Thomas Leiber | Fahrdynamiksystem, fahrzeug sowie verfahren zum betreiben eines fahrdynamiksystems |
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CN111322832A (zh) * | 2020-03-11 | 2020-06-23 | 苏州市兴鲁空分设备科技发展有限公司 | 全液体空分设备和工艺 |
CN114111218A (zh) * | 2020-08-25 | 2022-03-01 | 贵州盈德气体有限公司 | 空分液化压缩空气的一种新型节能工艺 |
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