CN115823825A - Air separation device and process for purifying oxygen and nitrogen by using air separation device - Google Patents

Air separation device and process for purifying oxygen and nitrogen by using air separation device Download PDF

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Publication number
CN115823825A
CN115823825A CN202211613181.6A CN202211613181A CN115823825A CN 115823825 A CN115823825 A CN 115823825A CN 202211613181 A CN202211613181 A CN 202211613181A CN 115823825 A CN115823825 A CN 115823825A
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China
Prior art keywords
air
tower
nitrogen
enters
molecular sieve
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CN202211613181.6A
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Chinese (zh)
Inventor
贾小虎
史亚军
郝彩云
左进春
曹玉凤
周伟
高磊
高鹏飞
苏得霆
韩芳
宋川楠
刘雪兵
卢刘波
张敬伟
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Jungar Dingcheng Gas Co ltd
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Jungar Dingcheng Gas Co ltd
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Priority to CN202211613181.6A priority Critical patent/CN115823825A/en
Publication of CN115823825A publication Critical patent/CN115823825A/en
Priority to CN202310292930.8A priority patent/CN116294433B/en
Pending legal-status Critical Current

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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04242—Cold end purification of the feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—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
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D46/00—Filters or filtering processes specially modified for separating dispersed particles from gases or vapours
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/0403—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of nitrogen
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
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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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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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
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
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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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04375—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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
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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
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—Start-up or control of the process; Details of the apparatus used
    • F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
    • F25J3/04951—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network
    • F25J3/04957—Arrangements of multiple air fractionation units or multiple equipments fulfilling the same process step, e.g. multiple trains in a network and inter-connecting equipments upstream of the fractionation unit (s), i.e. at the "front-end"
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/106—Silica or silicates
    • B01D2253/108—Zeolites
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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    • F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
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    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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    • F25J2220/02—Separating impurities in general from the feed stream
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    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/40—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being air
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    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/04—Multiple expansion turbines in parallel
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
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    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

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  • Chemical & Material Sciences (AREA)
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  • Oil, Petroleum & Natural Gas (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

The invention relates to the technical field of air separation, in particular to an air separation device and a process for purifying oxygen and nitrogen by using the air separation device. After raw material air of the device is filtered, compressed, precooled and purified, one part of the raw material air enters a booster compressor system, and the rest of the raw material air enters a lower tower; the pressurized air of the booster compressor system is divided into three strands, two strands are pumped out from the middle part for expansion and refrigeration and then enter the lower tower, and the third strand is led out from the final cooler and enters the lower tower; one part of the liquid nitrogen at the top of the lower tower is used as lower tower reflux liquid, the other part of the liquid nitrogen is stored, and the other part of the liquid nitrogen is used as upper tower reflux liquid; the waste liquid nitrogen at the lower part of the lower tower is cooled and then throttled to the upper part of the upper tower for rectification, and the oxygen-enriched liquid at the bottom of the lower tower is cooled and then throttled to the middle part of the upper tower for rectification; the low-pressure nitrogen at the top of the upper tower is reheated and then sent to a user pipe network, part of the reheated waste nitrogen is used as regeneration gas of a molecular sieve purification system, and the rest of the reheated waste nitrogen enters a water cooling tower; liquid oxygen is pumped out from the bottom of the main condensation evaporator, part of the liquid oxygen is stored, and the rest of the liquid oxygen is pressurized and reheated and then sent to a user pipe network. The invention can obviously reduce the energy consumption of the process.

Description

Air separation device and process for purifying oxygen and nitrogen by using air separation device
Technical Field
The invention relates to the technical field of air separation, in particular to an air separation device and a process for purifying oxygen and nitrogen by using the air separation device.
Background
An air separation plant is an industrial plant for separating the component gases in air to obtain gases such as oxygen, nitrogen, argon, etc. At present, the most common air separation method is cryogenic rectification, i.e. air is changed into liquid by adopting a compression cycle deep freezing method, and inert gases such as oxygen, nitrogen, argon and the like are gradually separated and produced from the liquid air through cryogenic rectification according to different boiling points of components in the air.
The principle of air rectification is as follows: due to the difference of boiling points, the evaporation sequence of oxygen, nitrogen and argon is as follows: nitrogen > argon > oxygen, the condensation sequence being: oxygen > argon > nitrogen; if the saturated vapor with higher temperature contacts the saturated liquid with lower temperature, the vapor emits heat and is partially condensed, and the liquid absorbs heat and is partially evaporated; when the steam is partially condensed, more high-boiling-point oxygen components in the steam are condensed into a liquid phase, and more low-boiling-point nitrogen components in the liquid phase are evaporated into a gas phase, so that the concentration of the nitrogen components in the gas phase is increased, and the concentration of the oxygen components in the liquid phase is increased; if the partial evaporation and partial condensation processes are carried out for a plurality of times, the concentration of the nitrogen component in the gas phase is continuously increased, and the concentration of the oxygen component in the liquid phase is continuously increased, so that the aim of separating the nitrogen from the oxygen is finally fulfilled. The main equipment for realizing rectification is a rectifying tower, each tower plate in the tower provides a place for partial evaporation and partial condensation due to once gas-liquid contact, and finally a high-purity nitrogen product is obtained at the tower top, and a high-purity oxygen product is obtained at the tower bottom.
Chinese patent publication No.: CN105466154B discloses an air separation process method, which belongs to the field of air separation and aims to solve the problem of low oxygen purity produced by the existing air separation process method. The process method comprises the following steps: 1. filtering air, then compressing the air in an air compressor, and cooling and washing the compressed air in a cooling tower; 2. one part of the purified air enters the bottom of the lower tower after being cooled to a dew point, the other part of the purified air flows into a booster compressor for boosting, the boosted air is divided into two paths, one path of air is sent into the upper tower after being expanded and refrigerated, and the other path of air flows into the lower tower after passing through a heat exchanger; 3. the air is primarily rectified in the lower tower, the liquid air enters the upper tower after passing through a cooler, one part of liquid oxygen is sent into a storage system, and the other part of liquid oxygen enters an oxygen pipe network after being reheated; 4. and extracting argon fraction from the middle part of the upper tower, sending the argon fraction into a crude argon tower, introducing pure nitrogen extracted from the top of the upper tower of the rectifying tower into a heat exchanger after passing through a cooler, and then sending the pure nitrogen into a water-cooling tower and a user pipe network. It can be seen that the invention has the following problems: the problem of high process energy consumption in the air separation process is not concerned.
Disclosure of Invention
Therefore, the invention provides an air separation device and a process for purifying oxygen and nitrogen by using the air separation device, which are used for solving the problem of high process energy consumption in the air separation process in the prior art.
In order to achieve the purpose, the invention provides an air separation device and a process for purifying oxygen and nitrogen by using the air separation device.
An air separation device comprises an air filtering system, an air compression system, an air precooling system, a molecular sieve purification system, a booster compressor system, a booster expander system and a fractionating tower system;
the air filtering system is used for filtering dust and mechanical impurities in raw air;
the air compression system is used for conveying the filtered air to the air pre-cooling system after the filtered air is subjected to multi-stage compression and is cooled by the interstage cooler;
the air pre-cooling system comprises an air cooling tower, a water cooling tower and a water cooling tower, wherein the air cooling tower is used for pre-cooling and washing air; the air sent by the air compressor passes through the air cooling tower from bottom to top to be cooled and washed, and then enters a molecular sieve purification system;
the molecular sieve purification system comprises a molecular sieve adsorber for adsorbing carbon dioxide, hydrocarbons and moisture in the air; after the air from the air cooling tower is purified by the molecular sieve adsorber, part of the purified air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of the purified air enters a low-pressure main heat exchanger of the fractionating tower;
the booster compressor system comprises a booster compressor, a first air inlet and a second air inlet, wherein the booster compressor is used for boosting purified air sent by the molecular sieve adsorber; the pressurized air is divided into three streams, wherein the first stream and the second stream of pressurized air are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; the third stream of pressurized air is led out from the final cooler of the booster compressor and enters a high-pressure main heat exchanger of the fractionating tower system;
the booster expansion machine system comprises two booster turbo expansion machines and two booster after-coolers, and the booster turbo expansion machines comprise booster machines and turbo expansion machines; the cooled pressurized air extracted from the middle part of the booster compressor enters a booster driven by a turboexpander for boosting, the boosted air enters a booster aftercooler for cooling, the cooled air enters a high-pressure main heat exchanger of a fractionating tower system, is cooled to a certain temperature by returned liquid oxygen, liquid nitrogen and waste nitrogen and then enters the turboexpander for expansion and refrigeration, and the air after expansion and refrigeration enters a lower tower of the fractionating tower system to participate in rectification;
the fractionating tower system comprises a low-pressure main heat exchanger, a high-pressure main heat exchanger, a lower tower, a main condensing evaporator, an upper tower, a subcooler, a liquid oxygen pump and a liquid nitrogen pump; air from a molecular sieve purification system enters a low-pressure main heat exchanger, is cooled to be close to a dew point by the returned nitrogen and waste nitrogen, and then is converged with the air after expansion refrigeration to enter a lower tower to participate in rectification; high-pressure air from a final cooler of a booster compressor enters a high-pressure main heat exchanger, is subjected to heat exchange liquefaction by the returned liquid oxygen, liquid nitrogen and waste nitrogen gas, is throttled and then enters a lower tower to participate in rectification; rectifying by a lower tower to obtain pure nitrogen at the top of the lower tower, feeding the pure nitrogen into a main condensation evaporator to be condensed by liquid oxygen in an upper tower, feeding part of the condensed liquid nitrogen into a liquid nitrogen pump for pressurization, feeding the part of the condensed liquid nitrogen into a high-pressure main heat exchanger for reheating, feeding the part of the condensed liquid nitrogen out of a cold box to serve as a nitrogen product, supercooling the rest of the condensed liquid nitrogen by a cooler, taking part of the condensed liquid nitrogen out of the cold box as a liquid nitrogen product, throttling the rest of the condensed liquid nitrogen, and feeding the rest of the condensed liquid nitrogen to the top of the upper tower as reflux liquid; obtaining waste liquid nitrogen at the lower part of the lower tower, and throttling the waste liquid nitrogen to the upper part of the upper tower to participate in rectification after the waste liquid nitrogen is supercooled by a cooler; oxygen-enriched liquid air is obtained at the bottom of the lower tower, is subcooled by a cooler and is throttled to the middle of the upper tower to participate in rectification; rectifying by an upper tower, reheating low-pressure nitrogen obtained at the top by a cooler and a main heat exchanger, sending the nitrogen to a nitrogen compressor unit for further compression, and sending the nitrogen to a user pipe network; after being reheated by a cooler and a main heat exchanger, the sewage nitrogen obtained at the upper part of the upper tower is cooled in a water cooling tower except for a part of sewage nitrogen used as regeneration gas of a molecular sieve purification system; liquid oxygen is pumped out from the bottom of the main condensation evaporator, one part of the liquid oxygen is taken as a liquid oxygen product and led out of the cold box, and the rest of the liquid oxygen is pressurized by a liquid oxygen pump, enters the main heat exchanger for reheating and then is sent to a user pipe network.
Further, the air precooling system also comprises a water cooling tower, a water chilling unit and a water pump;
the air cooling tower is a packed tower filled with two layers of tower materials, and a wire mesh separator is arranged at the top of the air cooling tower; the air sent by the air compressor passes through the air cooling tower from bottom to top, is cooled and washed by water from top to bottom, and finally passes through the wire mesh separator at the top to enter a molecular sieve purification system;
the chilled water entering the air cooling tower is divided into an upper section and a lower section, the lower section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump to enter the middle part of the air cooling tower and then flows out of the air cooling tower from top to bottom to return to a cooling water tower; the upper section is cooling water from a user circulating water system, and the cooling water is sent to the top of the air cooling tower after being subjected to heat and mass exchange cooling with waste nitrogen gas from the fractionating tower through a water cooling tower, pressurized by a water pump and further cooled by a water chilling unit.
Furthermore, the molecular sieve purification system comprises two molecular sieve adsorbers which are switched to work, and when one molecular sieve adsorber works, the other molecular sieve adsorber is regenerated and cold-blown for standby; the waste nitrogen from the fractionating tower is heated in a cascade mode by an electric heater and a steam heater, enters a molecular sieve adsorber for heating regeneration, moisture and CO2 in the molecular sieve adsorber are desorbed, after the heating regeneration of the molecular sieve adsorber is finished, the waste nitrogen from the fractionating tower is blown to be cold, and then the used waste nitrogen is discharged into the atmosphere.
Furthermore, the molecular sieve adsorber has a double-layer bed structure, wherein the bottom layer is an activated alumina bed layer, and the upper layer is a molecular sieve bed layer.
Furthermore, the air filtering system comprises a self-cleaning air filter, and self-cleaning can be realized by automatic timing and back blowing.
Further, the air compression system includes a turbine air compressor.
Further, the process comprises the following steps:
s01: raw material air enters an air filtering system to filter dust and mechanical impurities in the air, and the filtered air enters an air compression system;
s02: compressed air passes through an air cooling tower in an air pre-cooling system from bottom to top, and is washed while being cooled in the air cooling tower, so that clean air is obtained and enters a molecular sieve purification system;
s03: after the clean air from the air cooling tower is adsorbed by a molecular sieve purification system to remove carbon dioxide, hydrocarbon and moisture, a part of air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of air enters a low-pressure main heat exchanger of the fractionating tower;
s04: the washed air enters a molecular sieve purification system, after carbon dioxide, hydrocarbon and moisture in the air are removed by adsorption, a part of the air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of the air enters a low-pressure main heat exchanger of a fractionating tower, is cooled to be close to a dew point and then is converged with the air after expansion refrigeration to enter a lower tower for rectification;
s05: purified air sent by the molecular sieve purification system is pressurized in a booster compressor system to obtain pressurized air, the pressurized air is divided into three streams, and a first stream and a second stream of the pressurized air are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; leading out the third stream of pressurized air from a final cooler of the booster compressor, entering a high-pressure main heat exchanger of the fractionating tower system, liquefying and throttling the heat exchange, and then entering a lower tower to participate in rectification;
s06: the cooled pressurized air extracted from the middle part of the booster compressor enters a booster driven by a turboexpander for boosting, the boosted air enters a booster aftercooler for cooling, the cooled air enters a high-pressure main heat exchanger of a fractionating tower system, is cooled to a certain temperature by returned liquid oxygen, liquid nitrogen and waste nitrogen and then enters the turboexpander for expansion and refrigeration, and the air after expansion and refrigeration enters a lower tower of the fractionating tower system to participate in rectification;
s07: air is rectified by a lower tower of a fractionating tower to obtain pure nitrogen at the top of the lower tower, the pure nitrogen enters a main condensing evaporator and is condensed by upper tower liquid oxygen, one part of condensed liquid nitrogen is used as reflux liquid of the lower tower, one part of the condensed liquid nitrogen enters a liquid nitrogen pump for pressurization and is sent into a high-pressure main heat exchanger for reheating and then sent out of a cold box to be used as a nitrogen product, the rest of the condensed liquid nitrogen is subcooled by a cooler, one part of the condensed liquid nitrogen is taken as a liquid nitrogen product and is led out of the cold box, and the rest of the condensed liquid nitrogen is throttled and then sent to the top of the upper tower as reflux liquid;
obtaining waste liquid nitrogen at the lower part of the lower tower, and throttling the waste liquid nitrogen to the upper part of the upper tower to participate in rectification after the waste liquid nitrogen is supercooled by a cooler; oxygen-enriched liquid air is obtained at the bottom of the lower tower, is subcooled by a cooler and is throttled to the middle of the upper tower to participate in rectification;
rectifying by an upper tower, reheating low-pressure nitrogen obtained at the top by a cooler and a main heat exchanger, sending the nitrogen to a nitrogen compressor unit for further compression, and sending the nitrogen to a user pipe network; after being reheated by a cooler and a main heat exchanger, the sewage nitrogen obtained at the upper part of the upper tower is cooled in a water cooling tower except for a part of sewage nitrogen used as regeneration gas of a molecular sieve purification system; liquid oxygen is pumped out from the bottom of the main condensation evaporator, one part of the liquid oxygen is taken as a liquid oxygen product and led out of the cold box, and the rest of the liquid oxygen is pressurized by a liquid oxygen pump, enters the main heat exchanger for reheating and then is sent to a user pipe network.
Further, the air precooling system also comprises a water cooling tower, a water chilling unit and a water pump; the chilled water entering the air cooling tower is divided into an upper section and a lower section, the lower section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump to enter the middle part of the air cooling tower and then flows out of the air cooling tower from top to bottom to return to a cooling water tower; the upper section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump and further cooled by a water chilling unit after being subjected to heat-mass exchange cooling with waste nitrogen from a fractionating tower through a water cooling tower and then sent to the top of the air cooling tower.
Furthermore, the molecular sieve purification system comprises two molecular sieve adsorbers which are switched to work, and when one molecular sieve adsorber works, the other molecular sieve adsorber is regenerated and cold-blown for standby; the waste nitrogen from the fractionating tower is heated in cascade by an electric heater and a steam heater, and then enters a molecular sieve absorber for heating and regeneration to desorb water and CO in the molecular sieve absorber 2 After the molecular sieve adsorber is heated and regenerated, the waste nitrogen from the fractionating tower is blown to cool, and then the used waste nitrogen is discharged into the atmosphere.
Compared with the prior art, the device has the beneficial effects that after raw material air is filtered, compressed, precooled and purified, one part of the raw material air enters a booster compressor system, and the rest of the raw material air enters a lower tower; the pressurized air of the booster compressor system is divided into three strands, two strands are pumped out from the middle part for expansion and refrigeration and then enter the lower tower, and the third strand is led out from the final cooler and enters the lower tower; one part of the liquid nitrogen at the top of the lower tower is used as lower tower reflux liquid, the other part of the liquid nitrogen is stored, and the other part of the liquid nitrogen is used as upper tower reflux liquid; the waste liquid nitrogen at the lower part of the lower tower is cooled and then throttled to the upper part of the upper tower for rectification, and the oxygen-enriched liquid at the bottom of the lower tower is cooled and then throttled to the middle part of the upper tower for rectification; the low-pressure nitrogen at the top of the upper tower is reheated and then sent to a user pipe network, part of the reheated waste nitrogen is used as regeneration gas of a molecular sieve purification system, and the rest of the reheated waste nitrogen enters a water cooling tower; liquid oxygen is pumped out from the bottom of the main condensation evaporator, part of the liquid oxygen is stored, and the rest of the liquid oxygen is pressurized and reheated and then sent to a user pipe network. The invention obviously reduces the process energy consumption in the air separation process.
Drawings
Fig. 1 is a schematic view of the overall structure of an air separation plant according to an embodiment of the present invention;
FIG. 2 is a flow chart of a process for purifying oxygen and nitrogen using an air separation plant according to an embodiment of the present invention;
FIG. 3 is a process flow diagram of an air booster line of an air separation plant in accordance with an embodiment of the present invention;
fig. 4 is a process flow diagram of a nitrogen compression system of an air separation plant according to an embodiment of the present invention.
Detailed Description
In order that the objects and advantages of the invention will be more clearly understood, the invention is further described below with reference to examples; it should be understood that the specific embodiments described herein are merely illustrative of the invention and are not intended to limit the invention.
Preferred embodiments of the present invention are described below with reference to the accompanying drawings. It should be understood by those skilled in the art that these embodiments are only for explaining the technical principle of the present invention, and do not limit the scope of the present invention.
It should be noted that in the description of the present invention, the terms of direction or positional relationship indicated by the terms "upper", "lower", "left", "right", "inner", "outer", etc. are based on the directions or positional relationships shown in the drawings, which are only for convenience of description, and do not indicate or imply that the device or element must have a specific orientation, be constructed in a specific orientation, and be operated, and thus, should not be construed as limiting the present invention.
Furthermore, it should be noted that, in the description of the present invention, unless otherwise explicitly specified or limited, the terms "mounted," "connected," and "connected" are to be construed broadly, and may be, for example, fixedly connected, detachably connected, or integrally connected; can be mechanically or electrically connected; they may be connected directly or indirectly through intervening media, or they may be interconnected between two elements. The specific meanings of the above terms in the present invention can be understood by those skilled in the art according to specific situations.
Referring to fig. 1 to 4, which are schematic diagrams illustrating an overall structure of an air separation plant according to an embodiment of the present invention, fig. 2 is a process flow chart illustrating a process of purifying oxygen and nitrogen by using an air separation plant according to an embodiment of the present invention, fig. 3 is a process flow chart illustrating an air booster pipe of an air separation plant according to an embodiment of the present invention, and fig. 4 is a process flow chart illustrating a nitrogen compression system of an air separation plant according to an embodiment of the present invention.
The embodiment of the invention provides an air separation device which comprises an air filtering system, an air compression system, an air precooling system, a molecular sieve purification system, a booster compressor system, a booster expander system and a fractionating tower system.
The air filtering system is used for filtering dust and mechanical impurities in raw air;
the air compression system is used for conveying the filtered air to the air pre-cooling system after the filtered air is subjected to multi-stage compression and is cooled by the interstage cooler;
the air pre-cooling system comprises an air cooling tower, a water cooling tower and a water cooling tower, wherein the air cooling tower is used for pre-cooling and washing air; the air sent by the air compressor passes through the air cooling tower from bottom to top to be cooled and washed, and then enters a molecular sieve purification system;
the molecular sieve purification system comprises a molecular sieve adsorber for adsorbing carbon dioxide, hydrocarbons and moisture in the air; after the air from the air cooling tower is purified by the molecular sieve absorber, part of the air enters the booster compressor system for boosting and is used as instrument air and device air, and the rest of the air enters the low-pressure main heat exchanger of the fractionating tower;
the booster compressor system comprises a booster compressor, a first pressure sensor and a second pressure sensor, wherein the booster compressor is used for boosting the clean air sent by the molecular sieve adsorber; the pressurized air is divided into three streams, wherein the first stream and the second stream of pressurized air are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; the third stream of pressurized air is led out from the final cooler of the booster compressor and enters a high-pressure main heat exchanger of the fractionating tower system;
the booster expansion machine system comprises two booster turbo expansion machines and two booster after-coolers, and the booster turbo expansion machines comprise booster machines and turbo expansion machines; the pressurized air which is extracted from the booster compressor system and cooled is firstly fed into a booster driven by a turboexpander for boosting, the boosted air is fed into a booster aftercooler for cooling, the cooled air is fed into a high-pressure main heat exchanger of a fractionating tower system, is cooled to a certain temperature by the returned liquid oxygen, liquid nitrogen and waste nitrogen and then fed into the turboexpander for expansion and refrigeration, and the air after expansion and refrigeration is fed into a lower tower of the fractionating tower system to participate in rectification;
the fractionating tower system is used for fractionating and purifying oxygen and nitrogen in the air.
The component composition and the working process of each system are as follows:
(1) Air filtration system and air compression system
The air filtering system comprises a self-cleaning air filter, and self-cleaning can be realized by automatic timing back flushing;
the air compression system comprises a turbine air compressor;
the air containing dust raw materials enters a self-cleaning air filter to filter out mechanical particles, dust and the like in the air; the filtered air enters an air compression system again, is compressed to 0.61MPa.A by the air compression system and then enters an air precooling system.
(2) Air precooling system
The air precooling system mainly comprises an air cooling tower, a water chilling unit and four water pumps.
The air cooling tower is a packed tower filled with two layers of tower materials, and the top of the air cooling tower is provided with a wire mesh separator which can avoid liquid drops carried by precooled air;
air is sent to the bottom of the air cooling tower from an air compressor system, passes through the packing layer from bottom to top, is cooled by water from top to bottom, washes partial harmful impurities such as NOx, SO2, C1-and the like, finally passes through the wire mesh separator at the top, enters a molecular sieve purification system, and the temperature of the air discharged from the air cooling tower is about 15 ℃.
The water entering the air cooling tower is divided into two sections: the lower section is cooling water from a user circulating water system, and the cooling water is pressurized into the middle part of the air cooling tower by a cooling water pump and is discharged from the air cooling tower from top to bottom and returned to the water cooling tower; the upper section is cooling water from a user circulating water system, and after the cooling water is subjected to heat-mass exchange cooling with redundant waste nitrogen gas from the fractionating tower through a water cooling tower, the cooling water is pressurized by a chilled water pump and further cooled by a water chilling unit, and then the cooling water is sent to the top of the air cooling tower.
(3) Air purification system
The air purification system mainly comprises two adsorbers, a steam heater, an electric heater and a total emptying silencer.
The molecular sieve adsorber is of a horizontal double-bed structure, the lower layer is activated alumina, the upper layer is molecular sieve air from an air cooling tower, moisture, CO2 and other CnHm in the molecular sieve air are removed by the adsorber, a part of purified air enters a booster compressor to be boosted and is used as instrument air and device air, and the rest of the purified air enters a low-pressure main heat exchanger of a fractionating tower.
The molecular sieve adsorber is switched into two working modes: when one molecular sieve absorber works, the other molecular sieve absorber is regenerated and cold blown for standby; the waste nitrogen from the fractionating tower is heated to about 180 ℃ in a cascade mode through an electric heater and a steam heater, then enters a molecular sieve adsorber for heating and regeneration, the moisture and CO2 of the molecular sieve adsorber are desorbed, the waste nitrogen from the fractionating tower is blown to be cold after the regeneration is finished, and then the used waste nitrogen is discharged into the atmosphere.
The water content of the air purified by the molecular sieve adsorber is below the dew point of-65 ℃, and CO2 is less than or equal to 1PPm.
(4) Booster compressor system
The booster compressor system includes a booster compressor.
The clean air from the molecular sieve adsorber enters a booster compressor for boosting. The pressurized air is divided into three streams, wherein the first stream of pressurized air (the flow rate is 2700Nm3/h and the pressure is 1.2MPa.G) and the second stream of pressurized air (the flow rate is 17500Nm3/h and the pressure is 2.64MPa.G) are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; the third pressurized air (flow 29000Nm3/h, pressure 6.26MPa.G) is led out from the last stage of the booster compressor, and enters the high-pressure main heat exchanger of the fractionating tower system after being cooled.
(5) Booster expander system
The booster expansion machine system mainly comprises two booster turbo expansion machines, two booster aftercoolers and two oil supply devices; the booster turboexpander comprises a booster and a turboexpander;
the pressurized air which is extracted from the middle part of the booster compressor and cooled enters a booster driven by an expander to consume the energy output by the expander, so that the pressure of the air can be further improved, the pressurized air enters a booster aftercooler, enters a high-pressure main heat exchanger of a fractionating tower system after being cooled to the required temperature, is cooled to a certain temperature by the returned liquid oxygen, liquid nitrogen and waste nitrogen, enters a turbine expander for expansion and refrigeration, and the air after expansion and refrigeration enters a lower tower of the fractionating tower system to participate in rectification.
(6) Fractionating tower
The fractionating tower mainly comprises a low-pressure main heat exchanger, a high-pressure main heat exchanger, a lower tower, a main condensing evaporator, an upper tower, a subcooler, a liquid oxygen pump and a liquid nitrogen pump.
Air from a molecular sieve purification system enters a low-pressure main heat exchanger, is cooled to be close to a dew point by the returned nitrogen and waste nitrogen, and then is converged with the air after expansion refrigeration to enter a lower tower to participate in rectification; high-pressure air from a final cooler of a booster compressor enters a high-pressure main heat exchanger, is subjected to heat exchange liquefaction by the returned liquid oxygen, liquid nitrogen and waste nitrogen gas, is throttled and then enters a lower tower to participate in rectification;
rectifying by a lower tower to obtain pure nitrogen at the top of the lower tower, feeding the pure nitrogen into a main condensation evaporator to be condensed by liquid oxygen of an upper tower, feeding part of condensed liquid nitrogen as reflux liquid of the lower tower, feeding part of the condensed liquid nitrogen into a liquid nitrogen pump to be pressurized to 6.1MPa.G, feeding the part of the condensed liquid nitrogen into a high-pressure main heat exchanger to be reheated, feeding the reheated liquid nitrogen out of a cold box to serve as a nitrogen product, supercooling the rest of the condensed liquid nitrogen by a cooler, taking part of the condensed liquid nitrogen as a liquid nitrogen product out of the cold box, throttling the rest of the condensed liquid nitrogen, and feeding the throttled liquid nitrogen as reflux liquid of the upper tower to the top of the upper tower;
obtaining waste liquid nitrogen at the lower part of the lower tower, and throttling the waste liquid nitrogen to the upper part of the upper tower to participate in rectification after the waste liquid nitrogen is supercooled by a cooler; oxygen-enriched liquid air is obtained at the bottom of the lower tower, is subcooled by a cooler and is throttled to the middle of the upper tower to participate in rectification;
rectifying by an upper tower, reheating low-pressure nitrogen obtained at the top by a cooler and a main heat exchanger, sending the nitrogen to a nitrogen compressor unit for further compression, and sending the nitrogen to a user pipe network;
obtaining polluted nitrogen at the upper part of the upper tower, reheating the polluted nitrogen by a cooler and a main heat exchanger, and then, refrigerating the polluted nitrogen in a water cooling tower except for using a part of the polluted nitrogen as regeneration gas of a molecular sieve purification system;
liquid oxygen is pumped out from the bottom of the main condensation evaporator, one part of the liquid oxygen is taken as a liquid oxygen product and led out of the cold box, and the rest is pressurized to 6.3MPa by a liquid oxygen pump, enters the main heat exchanger for reheating and then is sent to a user for use.
The embodiment of the invention provides a process for purifying oxygen and nitrogen by using an air separation device, which comprises the following steps:
s01: raw material air enters an air filtering system to filter dust and mechanical impurities in the air, and the filtered air enters an air compression system;
s02: compressed air passes through an air cooling tower in an air pre-cooling system from bottom to top, and is washed while being cooled in the air cooling tower, so that clean air is obtained and enters a molecular sieve purification system;
s03: after the clean air from the air cooling tower is adsorbed by a molecular sieve purification system to remove carbon dioxide, hydrocarbon and moisture, a part of air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of air enters a low-pressure main heat exchanger of the fractionating tower;
s04: the washed air enters a molecular sieve purification system, after carbon dioxide, hydrocarbon and moisture in the air are removed by adsorption, a part of air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of air enters a low-pressure main heat exchanger of a fractionating tower, is cooled to be close to a dew point, then is converged with the air after expansion refrigeration, and enters a lower tower to participate in rectification;
s05: purified air sent by the molecular sieve purification system is pressurized in a booster compressor system to obtain pressurized air, the pressurized air is divided into three streams, and a first stream and a second stream of the pressurized air are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; leading out the third stream of pressurized air from a final cooler of the booster compressor, entering a high-pressure main heat exchanger of the fractionating tower system, liquefying and throttling the heat exchange, and then entering a lower tower to participate in rectification;
s06: the cooled pressurized air extracted from the middle part of the booster compressor enters a booster driven by a turboexpander for boosting, the boosted air enters a booster aftercooler for cooling, the cooled air enters a high-pressure main heat exchanger of a fractionating tower system, is cooled to a certain temperature by returned liquid oxygen, liquid nitrogen and waste nitrogen and then enters the turboexpander for expansion and refrigeration, and the air after expansion and refrigeration enters a lower tower of the fractionating tower system to participate in rectification;
s07: air is rectified by a lower tower of a fractionating tower, pure nitrogen is obtained at the top of the lower tower, the pure nitrogen enters a main condensation evaporator and is condensed by upper tower liquid oxygen, part of condensed liquid nitrogen is used as reflux liquid of the lower tower, part of condensed liquid nitrogen enters a liquid nitrogen pump for pressurization and is sent into a high-pressure main heat exchanger for reheating and then sent out of a cold box to be used as a nitrogen product, the rest of condensed liquid nitrogen is subcooled by a cooler, part of condensed liquid nitrogen is taken as a liquid nitrogen product and is led out of the cold box, and the rest of condensed liquid nitrogen is throttled and then sent to the top of the upper tower as reflux liquid;
obtaining waste liquid nitrogen at the lower part of the lower tower, and throttling the waste liquid nitrogen to the upper part of the upper tower to participate in rectification after the waste liquid nitrogen is supercooled by a cooler; oxygen-enriched liquid air is obtained at the bottom of the lower tower, is subcooled by a cooler and is throttled to the middle of the upper tower to participate in rectification;
rectifying by an upper tower, reheating low-pressure nitrogen obtained at the top by a cooler and a main heat exchanger, sending the nitrogen to a nitrogen compressor unit for further compression, and sending the nitrogen to a user pipe network; after being reheated by a cooler and a main heat exchanger, the sewage nitrogen obtained at the upper part of the upper tower is cooled in a water cooling tower except for a part of sewage nitrogen used as regeneration gas of a molecular sieve purification system; liquid oxygen is pumped out from the bottom of the main condensation evaporator, one part of the liquid oxygen is taken as a liquid oxygen product and led out of the cold box, and the rest of the liquid oxygen is pressurized by a liquid oxygen pump, enters the main heat exchanger for reheating and then is sent to a user pipe network.
In the embodiment of the invention, the air precooling system further comprises a water cooling tower, a water chilling unit and a water pump; the chilled water entering the air cooling tower is divided into an upper section and a lower section, the lower section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump to enter the middle part of the air cooling tower and then flows out of the air cooling tower from top to bottom to return to a cooling water tower; the upper section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump and further cooled by a water chilling unit after being subjected to heat-mass exchange cooling with waste nitrogen from a fractionating tower through a water cooling tower and then sent to the top of the air cooling tower.
In the embodiment of the invention, the molecular sieve purification system comprises two molecular sieve adsorbers which are switched to work, and when one molecular sieve adsorber works, the other molecular sieve adsorber is regenerated and cold-blown for standby; the waste nitrogen from the fractionating tower is heated in a cascade mode by an electric heater and a steam heater, enters a molecular sieve adsorber for heating regeneration, moisture and CO2 in the molecular sieve adsorber are desorbed, after the heating regeneration of the molecular sieve adsorber is finished, the waste nitrogen from the fractionating tower is blown to be cold, and then the used waste nitrogen is discharged into the atmosphere.
So far, the technical solutions of the present invention have been described in connection with the preferred embodiments shown in the drawings, but it is easily understood by those skilled in the art that the scope of the present invention is obviously not limited to these specific embodiments. Equivalent changes or substitutions of related technical features can be made by those skilled in the art without departing from the principle of the invention, and the technical scheme after the changes or substitutions can fall into the protection scope of the invention.
The above description is only a preferred embodiment of the present invention and is not intended to limit the present invention; various modifications and alterations to this invention will become apparent to those skilled in the art. Any modification, equivalent replacement, or improvement made within the spirit and principle of the present invention should be included in the protection scope of the present invention.

Claims (9)

1. An air separation device is characterized by comprising an air filtering system, an air compression system, an air precooling system, a molecular sieve purification system, a booster compressor system, a booster expander system and a fractionating tower system;
the air filtering system is used for filtering dust and mechanical impurities in raw air;
the air compression system is used for conveying the filtered air to the air pre-cooling system after the filtered air is subjected to multi-stage compression and is cooled by the interstage cooler;
the air pre-cooling system comprises an air cooling tower, a water cooling tower and a water cooling tower, wherein the air cooling tower is used for pre-cooling and washing air; the air sent by the air compressor passes through the air cooling tower from bottom to top to be cooled and washed, and then enters a molecular sieve purification system;
the molecular sieve purification system comprises a molecular sieve adsorber for adsorbing carbon dioxide, hydrocarbons and moisture in the air; after the air from the air cooling tower is purified by the molecular sieve adsorber, part of the purified air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of the purified air enters a low-pressure main heat exchanger of the fractionating tower;
the booster compressor system comprises a booster compressor, a first air inlet, a second air inlet and a first air outlet, wherein the booster compressor is used for boosting the purified air sent by the molecular sieve adsorber; the pressurized air is divided into three streams, wherein the first stream and the second stream of pressurized air are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; the third stream of pressurized air is led out from the final cooler of the booster compressor and enters a high-pressure main heat exchanger of the fractionating tower system;
the booster expansion machine system comprises two booster turboexpansion machines and two booster after-coolers, wherein the booster turboexpansion machines comprise a booster and a turboexpansion machine; the cooled pressurized air pumped out from the middle part of the booster compressor firstly enters a booster driven by a turboexpander for boosting, the boosted air enters a booster aftercooler for cooling, the cooled air enters a high-pressure main heat exchanger of a fractionating tower system, is cooled to a certain temperature by returned liquid oxygen, liquid nitrogen and waste nitrogen and then enters the turboexpander for expansion and refrigeration, and the air after expansion and refrigeration enters a lower tower of the fractionating tower system to participate in rectification;
the fractionating tower system comprises a low-pressure main heat exchanger, a high-pressure main heat exchanger, a lower tower, a main condensing evaporator, an upper tower, a subcooler, a liquid oxygen pump and a liquid nitrogen pump; air from a molecular sieve purification system enters a low-pressure main heat exchanger, is cooled to be close to a dew point by the returned nitrogen and waste nitrogen, and then is converged with the air after expansion refrigeration to enter a lower tower to participate in rectification; high-pressure air from a final cooler of a booster compressor enters a high-pressure main heat exchanger, is subjected to heat exchange liquefaction by the returned liquid oxygen, liquid nitrogen and waste nitrogen gas, is throttled and then enters a lower tower to participate in rectification; rectifying by a lower tower to obtain pure nitrogen at the top of the lower tower, feeding the pure nitrogen into a main condensation evaporator to be condensed by liquid oxygen in an upper tower, feeding part of the condensed liquid nitrogen into a liquid nitrogen pump for pressurization, feeding the part of the condensed liquid nitrogen into a high-pressure main heat exchanger for reheating, feeding the part of the condensed liquid nitrogen out of a cold box to serve as a nitrogen product, supercooling the rest of the condensed liquid nitrogen by a cooler, taking part of the condensed liquid nitrogen out of the cold box as a liquid nitrogen product, throttling the rest of the condensed liquid nitrogen, and feeding the rest of the condensed liquid nitrogen to the top of the upper tower as reflux liquid; obtaining waste liquid nitrogen at the lower part of the lower tower, and throttling the waste liquid nitrogen to the upper part of the upper tower to participate in rectification after the waste liquid nitrogen is supercooled by a cooler; oxygen-enriched liquid air is obtained at the bottom of the lower tower, is subcooled by a cooler and is throttled to the middle of the upper tower to participate in rectification; rectifying by an upper tower, reheating low-pressure nitrogen obtained at the top by a cooler and a main heat exchanger, sending the nitrogen to a nitrogen compressor unit for further compression, and sending the nitrogen to a user pipe network; after being reheated by a cooler and a main heat exchanger, the sewage nitrogen obtained at the upper part of the upper tower is cooled in a water cooling tower except for a part of sewage nitrogen used as regeneration gas of a molecular sieve purification system; liquid oxygen is pumped out from the bottom of the main condensation evaporator, one part of the liquid oxygen is taken as a liquid oxygen product and led out of the cold box, and the rest of the liquid oxygen is pressurized by a liquid oxygen pump, enters the main heat exchanger for reheating and then is sent to a user pipe network.
2. The air separation plant according to claim 1, wherein said air pre-cooling system further comprises a water cooling tower, a water chiller, and a water pump;
the air cooling tower is a packed tower filled with two layers of tower materials, and a wire mesh separator is arranged at the top of the air cooling tower; the air sent by the air compressor passes through the air cooling tower from bottom to top, is cooled and washed by water from top to bottom, and finally passes through the wire mesh separator at the top to enter a molecular sieve purification system;
the chilled water entering the air cooling tower is divided into an upper section and a lower section, the lower section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump to enter the middle part of the air cooling tower and then flows out of the air cooling tower from top to bottom to return to a cooling water tower; the upper section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump and further cooled by a water chilling unit after being subjected to heat-mass exchange cooling with waste nitrogen from a fractionating tower through a water cooling tower and then sent to the top of the air cooling tower.
3. The air separation plant according to claim 1, characterized in that the molecular sieve purification system comprises two molecular sieve adsorbers which are switched to work, and when one molecular sieve adsorber works, the other molecular sieve adsorber is regenerated and cold-blown for standby; the waste nitrogen from the fractionating tower is heated in a cascade mode by an electric heater and a steam heater, enters a molecular sieve adsorber for heating regeneration, water and CO2 in the molecular sieve adsorber are desorbed, after the heating regeneration of the molecular sieve adsorber is finished, the waste nitrogen from the fractionating tower is blown to be cold, and then the used waste nitrogen is discharged into the atmosphere.
4. The air separation plant according to claim 3, characterized in that the molecular sieve adsorber has a double-bed structure, wherein the bottom layer is an activated alumina bed layer and the upper layer is a molecular sieve bed layer.
5. An air separation plant according to claim 1, wherein the air filtration system comprises a self-cleaning air filter, which is self-cleaning by automatic timed back-flushing.
6. An air separation plant according to claim 1, wherein said air compression system includes a turbine air compressor.
7. A process for purifying oxygen and nitrogen using an air separation plant, using the air separation plant according to any one of claims 1 to 6, comprising the steps of:
s01: raw material air enters an air filtering system to filter dust and mechanical impurities in the air, and the filtered air enters an air compression system;
s02: compressed air passes through an air cooling tower in an air pre-cooling system from bottom to top, and is washed while being cooled in the air cooling tower, so that clean air is obtained and enters a molecular sieve purification system;
s03: after the clean air from the air cooling tower is adsorbed by a molecular sieve purification system to remove carbon dioxide, hydrocarbon and moisture, a part of air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of air enters a low-pressure main heat exchanger of the fractionating tower;
s04: the washed air enters a molecular sieve purification system, after carbon dioxide, hydrocarbon and moisture in the air are removed by adsorption, a part of air enters a booster compressor system for boosting and is used as instrument air and device air, and the rest of air enters a low-pressure main heat exchanger of a fractionating tower, is cooled to be close to a dew point, then is converged with the air after expansion refrigeration, and enters a lower tower to participate in rectification;
s05: purified air sent by the molecular sieve purification system is pressurized in a booster compressor system to obtain pressurized air, the pressurized air is divided into three streams, and a first stream and a second stream of the pressurized air are pumped out from the middle part of the booster compressor and enter a booster expander system after being cooled; leading out the third stream of pressurized air from a final cooler of the booster compressor, entering a high-pressure main heat exchanger of the fractionating tower system, liquefying and throttling the heat exchange, and then entering a lower tower to participate in rectification;
s06: the cooled pressurized air extracted from the middle part of the booster compressor enters a booster driven by a turboexpander for boosting, the boosted air enters a booster aftercooler for cooling, the cooled air enters a high-pressure main heat exchanger of a fractionating tower system, is cooled to a certain temperature by returned liquid oxygen, liquid nitrogen and waste nitrogen and then enters the turboexpander for expansion and refrigeration, and the air after expansion and refrigeration enters a lower tower of the fractionating tower system to participate in rectification;
s07: air is rectified by a lower tower of a fractionating tower to obtain pure nitrogen at the top of the lower tower, the pure nitrogen enters a main condensing evaporator and is condensed by upper tower liquid oxygen, one part of condensed liquid nitrogen is used as reflux liquid of the lower tower, one part of the condensed liquid nitrogen enters a liquid nitrogen pump for pressurization and is sent into a high-pressure main heat exchanger for reheating and then sent out of a cold box to be used as a nitrogen product, the rest of the condensed liquid nitrogen is subcooled by a cooler, one part of the condensed liquid nitrogen is taken as a liquid nitrogen product and is led out of the cold box, and the rest of the condensed liquid nitrogen is throttled and then sent to the top of the upper tower as reflux liquid;
obtaining waste liquid nitrogen at the lower part of the lower tower, and throttling the waste liquid nitrogen to the upper part of the upper tower to participate in rectification after the waste liquid nitrogen is supercooled by a cooler; oxygen-enriched liquid air is obtained at the bottom of the lower tower, is subcooled by a cooler and is throttled to the middle of the upper tower to participate in rectification;
rectifying by an upper tower, reheating low-pressure nitrogen obtained at the top by a cooler and a main heat exchanger, sending the nitrogen to a nitrogen compressor unit for further compression, and sending the nitrogen to a user pipe network; after being reheated by a cooler and a main heat exchanger, the sewage nitrogen obtained at the upper part of the upper tower is cooled in a water cooling tower except for a part of sewage nitrogen used as regeneration gas of a molecular sieve purification system; liquid oxygen is pumped out from the bottom of the main condensation evaporator, one part of the liquid oxygen is taken as a liquid oxygen product and led out of the cold box, and the rest of the liquid oxygen is pressurized by a liquid oxygen pump, enters the main heat exchanger for reheating and then is sent to a user pipe network.
8. The process of claim 7, wherein the air pre-cooling system further comprises a water cooling tower, a water chiller, and a water pump; the chilled water entering the air cooling tower is divided into an upper section and a lower section, the lower section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump to enter the middle part of the air cooling tower and then flows out of the air cooling tower from top to bottom to return to a cooling water tower; the upper section is cooling water from a user circulating water system, and the cooling water is pressurized by a water pump and further cooled by a water chilling unit after being subjected to heat-mass exchange cooling with waste nitrogen from a fractionating tower through a water cooling tower and then sent to the top of the air cooling tower.
9. The process of claim 7, wherein the molecular sieve purification system comprises two molecular sieve adsorbers, and when one molecular sieve adsorber works, the other molecular sieve adsorber is regenerated and cold-blown for standby; the waste nitrogen from the fractionating tower is heated in a cascade mode by an electric heater and a steam heater, enters a molecular sieve adsorber for heating regeneration, moisture and CO2 in the molecular sieve adsorber are desorbed, after the heating regeneration of the molecular sieve adsorber is finished, the waste nitrogen from the fractionating tower is blown to be cold, and then the used waste nitrogen is discharged into the atmosphere.
CN202211613181.6A 2022-12-15 2022-12-15 Air separation device and process for purifying oxygen and nitrogen by using air separation device Pending CN115823825A (en)

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