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CN109297258A - A method for reducing gas emission and pipe network pressure in an air separation plant - Google Patents

A method for reducing gas emission and pipe network pressure in an air separation plant Download PDF

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Publication number
CN109297258A
CN109297258A CN201811095677.2A CN201811095677A CN109297258A CN 109297258 A CN109297258 A CN 109297258A CN 201811095677 A CN201811095677 A CN 201811095677A CN 109297258 A CN109297258 A CN 109297258A
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CN
China
Prior art keywords
air separation
gas
separation unit
product
air
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Granted
Application number
CN201811095677.2A
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Chinese (zh)
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CN109297258B (en
Inventor
王立
张培昆
浦碧露
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University of Science and Technology Beijing USTB
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University of Science and Technology Beijing USTB
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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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
    • F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
    • F25J3/04618—Heat exchange integration with process streams, e.g. from the air gas consuming unit for cooling an air stream fed to the air fractionation unit
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04678—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser cooled by oxygen enriched liquid from high pressure column bottoms
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04642—Recovering noble gases from air
    • F25J3/04648—Recovering noble gases from air argon
    • F25J3/04654—Producing crude argon in a crude argon column
    • F25J3/04666—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system
    • F25J3/04672—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser
    • F25J3/04703—Producing crude argon in a crude argon column as a parallel working rectification column of the low pressure column in a dual pressure main column system having a top condenser being arranged in more than one vessel
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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
    • F25J3/04763—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
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
    • 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
    • F25J3/04763—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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • 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
    • F25J2210/04—Mixing or blending of fluids with the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/02—Compressor intake arrangement, e.g. filtering or cooling
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/58—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being argon or crude argon
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/42—Processes or apparatus involving steps for recycling of process streams the recycled stream being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen

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

Abstract

The present invention provides the method for a kind of reduction air separation unit gas release and ductwork pressure, belongs to spatial division technology field.This method in air separation unit by adding from product oxygen outlet conduit to the reflux line of air compressor machine entrance and from product nitrogen gas outlet conduit to the reflux line of air compressor machine entrance, and control valve is set in the two pipelines and reduces the period in gas consumer dosage to realize, by the gas backstreaming of air separation unit portioned product into air separation unit unstripped gas, it improves return product gas and holds the mean concentration in doses in air separation column, by portion gas product reflux into air separation unit unstripped gas, it realizes due to the fluctuation of gas consumer dosage and the buffer storage of product gas more than needed in air separation unit.This method had not only reduced the release of gas products, but also reduced ductwork pressure and air separation unit energy consumption.In addition to increasing reflux line, do not increase any other new equipment, do not change air compressor machine load and decrement, ensure that the safety and stability of air separation plant operation.

Description

A method of reducing the release of air separation unit gas and ductwork pressure
Technical field
The present invention relates to spatial division technology fields, particularly relate to the side of a kind of reduction air separation unit gas release and ductwork pressure Method.
Background technique
Chinese output of steel ranks first in the world in place since nineteen ninety-six, and steel industry is huge to the demand of industrial gasses, If Chinese crude steel yield in 2013 is 779.04Mt, oxygen consumption reaches (7.79~10.91) × 1010m3.Iron and steel enterprise is general All over industrial gasses are produced using Deep Cooling Method space division process, with the gradually growth of iron and steel output, the scale of air separation unit is also towards big Typeization development.Device is bigger, and Unit consumption for oxygen production (power consumption) is lower.However, discontinuity and fluctuation is presented with gas demand, this and sky Separating device duration is stablized gas supply and is contradicted, and then leads to gas products release and the high phenomenon of energy consumption occur.
Due to the imbalance between supply and demand between space division continuous production and STEELMAKING PRODUCTION discontinuity, on the one hand will cause in low dosage The release of section product gas, and the average pressure of gas pipeline network can be made to increase, cause system energy consumption to increase.The reality of the method for the present invention It applies, to the bleeding rate and ductwork pressure for reducing air separation unit gas products, the production energy consumption that maximizing reduces air separation unit has Important function.In addition, doing experiment to be pressed into 30% oxygen content before blast furnace blower according to associated mechanisms is that comparison is safe, pressure Entering less can be dangerous within 27% oxygen content.So oxygen flows back into the oxygen content of air compressor machine 27% hereinafter, being peace Complete.
Summary of the invention
The technical problem to be solved in the present invention is to provide the methods of a kind of reduction air separation unit gas release and ductwork pressure.
This method specifically:
Firstly, adding the reflux line from product oxygen outlet conduit to air compressor machine entrance in air separation unit, and in pipe Control valve is set in road；
Secondly, adding the reflux line from product nitrogen gas outlet conduit to air compressor machine entrance in air separation unit, and in pipe Control valve is set in road；
Again, increase tower tower reactor volume under air separation unit；
Finally, the period is reduced in gas consumer dosage, by air separation unit portioned product gas backstreaming when air separation unit is run Into air separation unit unstripped gas, return product gas is improved in air separation column and holds the mean concentration in doses, is realized due to gas consumer Dosage fluctuates and the buffer storage of product gas more than needed in air separation unit.
Wherein, the portioned product gas backstreaming is into air separation unit unstripped gas, is the fluctuation of gas consumer dosage and rich Remaining product gas is transmitted back to air separation unit unstripped gas entrance by reflux line and valve.
Buffer storage of the portioned product gas in air separation unit is when air separation unit product gas since gas consumer is used Amount fluctuation and when supply exceed demand, reduce the product gas output quantity, which be transmitted back to air separation unit air compressor machine and is entered In mouth raw air, the concentration of the product gas component in tower air is improved, to improve the product in full tower gas and liquid The mean concentration of gas component, namely improve the amount of holding of the product gas component in air separation unit；When consumer products gas dosage restore and When increase, then the yield and output quantity of the air separation unit product gas are improved, to meet user demand, while making should in air separation unit The product gas component amount of holding reduces and is restored to nominal situation level.In the process, rectifying column functions as the production The surge tank of product gas.
When air separation unit oxygen product since oxygen gas user is fluctuated when supply exceed demand, oxygen product output is reduced Superfluous oxygen is transmitted back in air separation unit unstripped gas by amount by reflux line and valve, reduces Oxygen venting.
When air separation unit nitrogen product since nitrogen gas user is fluctuated when supply exceed demand, nitrogen product output is reduced Superfluous nitrogen is transmitted back in air separation unit unstripped gas by amount by reflux line and valve, reduces nitrogen release.
In order to improve buffer-stored amount of the return product gas in tower, it can design and increase tower tower reactor appearance under air separation unit Product, the volume of holding of tower reactor liquid air, improves the buffer capacity or buffer capacity to return product gas when being operated normally by improving space division Power.
This method is suitable for external compression air separation unit and interior compression air separation device.
The advantageous effects of the above technical solutions of the present invention are as follows:
In above scheme, so that rectifying column is played the role of surge tank by the reflux of product gas, both reduce gas products Release, and reduce ductwork pressure and air separation unit energy consumption.Other than increasing reflux line, does not increase any other and newly set It is standby, do not change air compressor machine load and decrement, while ensure that the safety and stability of air separation plant operation.Due to the sky of production Gas total amount is constant, and refrigerating capacity is constant, thus process response lag be it is small, adjustment reaction speed it is fast.
Detailed description of the invention
Fig. 1 is 20000Nm in the embodiment of the present invention3The external compression air separation unit product gas reflux technique process of/h is illustrated Figure.
Wherein: 1- air filter；2- air compressor machine；3- air cooling tower；4- water cooler；5- water-cooling tower；6- silencer；7- points Son sieve absorber；8- steam heater；9- booster expansion turbine；10- main heat exchanger；The upper tower of 11-；12- master is cold；Tower under 13-； 14- subcooler；15- crude argon I tower；16- circulating pump；17- crude argon II tower；18- pure argon column；The spare electric heater of 19-.
Specific embodiment
To keep the technical problem to be solved in the present invention, technical solution and advantage clearer, below in conjunction with attached drawing and tool Body embodiment is described in detail.
The present invention be solve it is existing as gas consumer dosage fluctuation and caused by air separation unit product gas release and pipe network The high problem of pressure provides the method for a kind of reduction air separation unit gas release and ductwork pressure.
This method specifically:
Firstly, adding the reflux line from product oxygen outlet conduit to air compressor machine entrance in air separation unit, and in pipe Control valve is set in road；
Secondly, adding the reflux line from product nitrogen gas outlet conduit to air compressor machine entrance in air separation unit, and in pipe Control valve is set in road；
Again, increase tower tower reactor volume under air separation unit；
Finally, the period is reduced in gas consumer dosage, by air separation unit portioned product gas backstreaming when air separation unit is run Into air separation unit unstripped gas, return product gas is improved in air separation column and holds the mean concentration in doses, is realized due to gas consumer Dosage fluctuates and the buffer storage of product gas more than needed in air separation unit.
It is explained combined with specific embodiments below.
As shown in Figure 1, being 20000Nm3The external compression air separation unit product gas reflux technique flow diagram of/h, in the sky In separating device, air enters air compressor machine 2 by air filter 1, is cooled down and is dehumidified subsequently into air cooling tower 3, air cooling tower 3 Water source cool down from water-cooling tower 5 and by water cooler 4.3 air of air cooling tower enters molecular sieve adsorber 7 and is inhaled out Echo purifying.Silencer 6 is set at molecular sieve adsorber 7.The regeneration gas of molecular sieve adsorber 7 be the pure nitrogen gas from pipe network simultaneously It is heated through steam heater 8 and spare electric heater 19.It exchanges heat by the air a part adsorbed and purified through main heat exchanger 10 Enter lower tower 13 afterwards, a part enters main heat exchanger 10 after the pressurization of booster expansion turbine 9, and takes out in the middle part of main heat exchanger 10 Enter after booster expansion turbine 9 expands out and enters upper tower 11.Heat exchange is carried out by main cold 12 between upper tower 11 and lower tower 13, Realize the evaporation of the 11 bottom liquid oxygen of condensation and upper tower of lower 13 top nitrogen of tower.Air passes through rectifying in lower tower 13 and upper tower 11 Realize the separation of oxygen nitrogen.Oxygen is extracted out from upper 11 lower part of tower and is sent into oxygen pipe network after 10 re-heat of main heat exchanger.Nitrogen is from Shang Ta 11 top extractions, are sent into Nitrogen pipe network after 10 rewarming of subcooler 14 and main heat exchanger.Argon fraction extracted out in the middle part of upper tower 11 into Enter crude argon I tower 15, the Argon fraction after preliminary purification is extracted out at the top of crude argon I tower 15 enters crude argon II tower 17, and crude argon is from thick Enter in the middle part of pure argon column 18 after being extracted out at the top of argon II tower 17 and carry out rectifying, and obtains pure liquid argon from 18 bottom of pure argon column.Crude argon II The kettle liquid of tower 17 returns to through circulating pump 16 and is used as phegma at the top of crude argon I tower 15.
This method in the oxygen pipe network of above-mentioned apparatus by adding from product oxygen outlet conduit to air compressor machine entrance Reflux line, and control valve is set in the duct and adds to enter from product nitrogen gas outlet conduit to air compressor machine in Nitrogen pipe network The reflux line of mouth, and control valve is set in the duct.
When gas consumer flow of oxygen is reduced, by the way that portioned product oxygen through reflux line and valve, is transmitted back to sky In the space division raw air of press entrance, realize since the product oxygen that gas consumer oxygen consuming amount fluctuates and has more than needed is in air separation unit Interior buffer storage, and the influence that product oxygen flows back to nitrogen gas purity can be offset by reducing nitrogen output.
When gas consumer nitrogen use level is reduced, by the way that portioned product nitrogen through reflux line and valve, is transmitted back to sky In the space division raw air of press entrance, realize since the product nitrogen gas that gas consumer is fluctuated with nitrogen quantity and is had more than needed is in air separation unit Interior buffer storage, and the influence that product nitrogen gas flows back to oxygen purity can be offset by reducing oxygen output.
In product gas reflux, Argon fraction can also be carried out by adjusting into upper 11 oxygen-enriched liquid air of tower and liquid nitrogen ratio It adjusts.
It is main when oxygen product reflux 0% to 20% under conditions of guaranteeing that oxygen output is constant by taking oxygen flows back as an example The variation of parameter is wanted to be shown in Table 1.Notice that the reflux ratio in following all tables refers to that the flow of reflux oxygen product accounts for oxygen production The ratio of product flow.
When 1. oxygen product of table reflux 0% to 20%, the variation of major product parameter
When oxygen reflux, the concentration of nitrogen product reduces the requirement for being unsatisfactory for product design, can suitably reduce nitrogen The yield of product guarantees that the purity of product is met the requirements.When oxygen product reflux 0% to 20%, to guarantee nitrogen product purity The change of production of nitrogen product is shown in Table 2.
When 2. oxygen product of table reflux 0% to 20%, for the change of production for guaranteeing nitrogen product purity nitrogen product
When using oxygen reflux technique, the volume for suitably increasing tower tower reactor under air separation unit can increase air separation unit Oxygen buffering capacity.20000Nm3The volume of tower tower reactor is 10m under/h air separation unit3.Table 3 is when oxygen product reflux 0% to 20% When, increase the oxygen buffering capacity (m of tower reactor corresponding to tower tower reactor volume under air separation unit3)。
When 3. oxygen product of table reflux 0% to 20%, the oxygen of tower reactor corresponding to tower tower reactor volume is slow under air separation unit Momentum (m3)
The above is a preferred embodiment of the present invention, it is noted that for those skilled in the art For, without departing from the principles of the present invention, several improvements and modifications can also be made, these improvements and modifications It should be regarded as protection scope of the present invention.

Claims (6)

1.一种降低空分装置气体放散和管网压力的方法，其特征在于：该方法具体如下：1. a method for reducing air separation plant gas emission and pipe network pressure, is characterized in that: the method is specifically as follows: 首先，在空分装置中增设从产品氧气出口管道到空压机入口的回流管道，并在管道中设置调节阀门；First, add a return pipeline from the product oxygen outlet pipeline to the air compressor inlet in the air separation unit, and set up a regulating valve in the pipeline; 其次，在空分装置中增设从产品氮气出口管道到空压机入口的回流管道，并在管道中设置调节阀门；Secondly, add a return pipeline from the product nitrogen outlet pipeline to the air compressor inlet in the air separation unit, and set up a regulating valve in the pipeline; 再次，增加空分装置下塔塔釜容积；Again, increase the volume of the lower tower kettle of the air separation unit; 最后，空分装置运行时，在气体用户用量减少时段，将空分装置部分产品气体回流到空分装置原料气中，提高回流产品气在空分塔持料量中的平均浓度，实现由于气体用户用量波动而富余的产品气在空分装置内的缓冲储存。Finally, when the air separation unit is running, during the period when the gas user consumption is reduced, part of the product gas of the air separation unit is refluxed into the raw gas of the air separation unit, so as to increase the average concentration of the refluxed product gas in the air separation tower holding capacity, and realize the gas Buffer storage of surplus product gas in the air separation unit with fluctuating user usage. 2.根据权利要求1所述的降低空分装置气体放散和管网压力的方法，其特征在于：所述的部分产品气体回流到空分装置原料气中，是指气体用户用量波动而富余的产品气体通过回流管道和阀门回送到空分装置原料气入口。2. The method for reducing the gas emission and pipe network pressure of an air separation plant according to claim 1, wherein the part of the product gas is returned to the raw material gas of the air separation plant, which means that the gas user consumption fluctuates and is surplus. The product gas is returned to the feed gas inlet of the air separation unit through the return line and valve. 3.根据权利要求1所述的降低空分装置气体放散和管网压力的方法，其特征在于：所述的增加空分装置下塔塔釜容积，是通过提高空分装置正常运行时塔釜液空的持有量，提高对回流产品气的缓冲容量或缓冲能力。3. the method for reducing air separation unit gas emission and pipe network pressure according to claim 1, is characterized in that: described increasing the lower tower still volume of the air separation unit is by increasing the tower still during normal operation of the air separation unit The holding capacity of air liquid increases the buffer capacity or buffer capacity of the returning product gas. 4.根据权利要求1所述的降低空分装置气体放散和管网压力的方法，其特征在于：当空分装置氧气产品由于氧气气体用户波动而供大于求时，减少氧气产品输出量，将过剩的氧气通过回流管道和阀门回送到空分装置原料气中，减少氧气放散。4. the method for reducing air separation unit gas emission and pipe network pressure according to claim 1, is characterized in that: when air separation unit oxygen product is oversupplied due to the fluctuation of oxygen gas users, reduce the output of oxygen product, the excess The oxygen is returned to the feed gas of the air separation unit through the return pipeline and valve to reduce the oxygen emission. 5.根据权利要求1所述的降低空分装置气体放散和管网压力的方法，其特征在于：当空分装置氮气产品由于氮气气体用户波动而供大于求时，减少氮气产品输出量，将过剩的氮气通过回流管道和阀门回送到空分装置原料气中，减少氮气放散。5. the method for reducing air separation unit gas emission and pipe network pressure according to claim 1, is characterized in that: when air separation unit nitrogen product is oversupplied due to the fluctuation of nitrogen gas users, reduce nitrogen product output, and excess The nitrogen is returned to the raw gas of the air separation unit through the return pipeline and valve to reduce the nitrogen emission. 6.根据权利要求1所述的降低空分装置气体放散和管网压力的方法，其特征在于：该方法适用于外压缩空分装置和内压缩空分装置。6 . The method for reducing the gas emission and pipe network pressure of an air separation plant according to claim 1 , wherein the method is suitable for an external compressed air separation plant and an internal compressed air separation plant. 7 .
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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110985887A (en) * 2019-11-08 2020-04-10 北京科技大学 Energy-saving method and system for reducing energy consumption of oxygen pipe network transmission and distribution system
US12104850B2 (en) 2021-05-06 2024-10-01 Air Products And Chemicals, Inc. Fluid recovery process and apparatus for xenon and or krypton recovery

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3191393A (en) * 1959-12-30 1965-06-29 Air Reduction Krypton-xenon separation from a gas mixture
US4285709A (en) * 1977-09-30 1981-08-25 Cleanair Combustion Systems, Ltd. Liquefactor
DE4425712A1 (en) * 1994-07-20 1996-01-25 Umsicht Inst Umwelt Sicherheit Process for the enrichment of the methane content of a mine gas
CN103123203A (en) * 2013-02-22 2013-05-29 河南开元空分集团有限公司 Method of preparing pure nitrogen by using exhaust gas with nitrogen to carry out once-more cryogenic distillation
CN203432210U (en) * 2013-09-11 2014-02-12 哈尔滨黎明气体有限公司 Efficient and energy-saving device capable of increasing high-purity liquid nitrogen yield in overall liquid air separation plant
CN104061756A (en) * 2014-06-09 2014-09-24 杭州杭氧股份有限公司 Method and device for producing belt pressure nitrogen product by coupling backflow dirty nitrogen entering pressure tower through part expansion refrigeration and part pressure boosting
JP2014214901A (en) * 2013-04-23 2014-11-17 Ｊｆｅスチール株式会社 Refined gas supply device and method for compensating purity of manufactured gas
CN105143801A (en) * 2013-03-28 2015-12-09 林德股份公司 Method and device for producing gaseous compressed oxygen having variable power consumption
CN107300295A (en) * 2017-03-06 2017-10-27 杭州杭氧股份有限公司 A kind of use raw nitrogen gas Deep Cooling Method produces the device and method of High Purity Nitrogen product

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3191393A (en) * 1959-12-30 1965-06-29 Air Reduction Krypton-xenon separation from a gas mixture
US4285709A (en) * 1977-09-30 1981-08-25 Cleanair Combustion Systems, Ltd. Liquefactor
DE4425712A1 (en) * 1994-07-20 1996-01-25 Umsicht Inst Umwelt Sicherheit Process for the enrichment of the methane content of a mine gas
CN103123203A (en) * 2013-02-22 2013-05-29 河南开元空分集团有限公司 Method of preparing pure nitrogen by using exhaust gas with nitrogen to carry out once-more cryogenic distillation
CN105143801A (en) * 2013-03-28 2015-12-09 林德股份公司 Method and device for producing gaseous compressed oxygen having variable power consumption
JP2014214901A (en) * 2013-04-23 2014-11-17 Ｊｆｅスチール株式会社 Refined gas supply device and method for compensating purity of manufactured gas
CN203432210U (en) * 2013-09-11 2014-02-12 哈尔滨黎明气体有限公司 Efficient and energy-saving device capable of increasing high-purity liquid nitrogen yield in overall liquid air separation plant
CN104061756A (en) * 2014-06-09 2014-09-24 杭州杭氧股份有限公司 Method and device for producing belt pressure nitrogen product by coupling backflow dirty nitrogen entering pressure tower through part expansion refrigeration and part pressure boosting
CN107300295A (en) * 2017-03-06 2017-10-27 杭州杭氧股份有限公司 A kind of use raw nitrogen gas Deep Cooling Method produces the device and method of High Purity Nitrogen product

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN110985887A (en) * 2019-11-08 2020-04-10 北京科技大学 Energy-saving method and system for reducing energy consumption of oxygen pipe network transmission and distribution system
CN110985887B (en) * 2019-11-08 2020-12-22 北京科技大学 An energy-saving method and system for reducing energy consumption of an oxygen pipe network transmission and distribution system
US12104850B2 (en) 2021-05-06 2024-10-01 Air Products And Chemicals, Inc. Fluid recovery process and apparatus for xenon and or krypton recovery

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