CN1320798A - Method and apparatus for low-temp. separation of air to produce compressed products - Google Patents

Method and apparatus for low-temp. separation of air to produce compressed products Download PDF

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Publication number
CN1320798A
CN1320798A CN01109513A CN01109513A CN1320798A CN 1320798 A CN1320798 A CN 1320798A CN 01109513 A CN01109513 A CN 01109513A CN 01109513 A CN01109513 A CN 01109513A CN 1320798 A CN1320798 A CN 1320798A
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pressure
air stream
feed air
column
mixing column
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CN1179181C (en
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罗特曼·迪特里希
孔茨·克里斯蒂安
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Linde GmbH
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Linde GmbH
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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
    • 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
    • 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
    • F25J3/04006—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
    • F25J3/04024—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 purified feed air, so-called boosted 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
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04109—Arrangements of compressors and /or their drivers
    • F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
    • 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
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • 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
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • 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
    • F25J3/0446—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 the heat generated by mixing two different phases
    • F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid oxygen
    • 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
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
    • F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • 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
    • F25J2245/40—Processes or apparatus involving steps for recycling of process streams the recycled stream being air

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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)
  • Oxygen, Ozone, And Oxides In General (AREA)

Abstract

The present invention relates to a process and an apparatus for producing a pressurized product by low-temperature fractionation of air in a rectification system composed of a high-pressure column (13) and a low-pressure column (14). A total airstream which comprises the first and second feed air streams is compressed to a first pressure (P<1>) which is lower than the operating pressure (P<HDS>) of the high-pressure column and is purified at about this first pressure (P<1>). The total purified airstream is divided into the first and the second feed airstream. The first feed airstream is further compressed separately from the second feed airstream to a second pressure (P<2>) which is at least equal to the operating pressure (P<HDS>) of the high-pressure column.

Description

The method and apparatus of air low temperature separation of produced compressed products
The present invention relates to a kind of method that adopts Cryogenic air separation from the gaseous compressed product that mixing column is produced according to claim 1, to produce compressed products.In the present invention, the mixing column operating pressure is lower than the operating pressure that nitrogen-oxygen separates used two Tower System mesohigh towers.
Distillation system of the present invention can build up two Tower Systems, for example Jing Dian double tower system; But also can be three towers or multitower system.Except nitrogen-oxygen knockout tower, may produce the especially facility of rare gas (as krypton, xenon and/or argon) of other constituent of air in addition.
As the oxygen enrichment cut of mixing column raw material, oxygen concentration is higher than airborne oxygen concentration, for example can reach 70%～99.5mol%, preferred 90%～98mol%.Mixing column is a column for counter-currently contacting, the liquid fraction counter current contacting that gaseous fraction that volatility is stronger and volatility are relatively poor.
The present invention is particularly suited for producing gaseous state unpure oxygen with pressure.The meaning of unpure oxygen is that oxygen content is 99.5mol% or lower, the mixture of 70%～99.5mol% particularly herein.The pressure of products obtained therefrom is for example 2.2～4.9 to cling to preferred 2.5～4.5 crust.Clearly, if desired, this compressed products can further compression under gaseous state.
It is open in EP697576A1 to start described these class methods and facility.Whole air are compressed to the pressure of about high-pressure tower in this patent, use a part of mixing column air expansion working then, make the mixing column air expand into the operating pressure of mixing column.Adopt this method, although the high pressure of this part air stream can be used for freezing, this method is all unfavorable to conserve energy in all cases.
The objective of the invention is to provide energy consumption low especially, the described method of beginning and relevant device.
The objective of the invention is to realize in the following way: total air stream that will comprise first, second feed air stream at least is compressed to and is lower than high-pressure tower operating pressure (P HDS) the first pressure (P 1); And greatly about this first pressure (P 1) under purify; Total air stream after the purification is divided into first and second feed air stream; First feed air stream of separating with second feed air stream further is compressed to the second pressure (P 2), this pressure equals the operating pressure (P of high-pressure tower at least HDS).
Therefore, total air stream does not really want to be compressed to system's maximum pressure, but is compressed to a lower value.And need the air of the sort of of elevated pressures or those air cuts, particularly high-pressure tower, further be compressed to desired value separately.Like this, method of the present invention is when the compression feeding air, and energy consumption can be accomplished low as much as possible.
If first pressure approximates the mixing column operating pressure greatly, just can realize minimum equipment cost.In this case, mixing column air (second feed air stream) need not further to change pressure and just can introduce mixing column.
Perhaps, first pressure can be lower than mixing column operating pressure (P MiS).In this case, second feed air stream of having separated with first feed air stream will further be compressed to the 3rd pressure (P 3), this pressure equals mixing column operating pressure (P at least MiS).
Preferably, before introducing mixing column, liquid band is pressed the oxygen enrichment cut to flow to overfire air and is connect heating in the ranks.For example overfire air stream can be the part of feeding air, and its pressure is in the pressure of high-pressure tower.This air stream is to take out under the medium temperature of main heat exchanger, and feeding air is cooled to about dew point in main heat exchanger; Said air stream need not further to change temperature just can carry out indirect heat exchange with oxygen enriched liquid.Adopt this mode, the temperature that enters the liquid of mixing column can form optimum Match with the condition of countercurrent mass transfer in the mixing column.
In the inventive method, by the 3rd feed air stream expansion working and introduce lower pressure column, freeze in best mode.Like this, can utilize " nature " pressure drop between first pressure and other pressure to remedy adiabatic loss,, make a part of product liquefaction if perhaps suitable.
Preferably, the 3rd feed air stream recompressed before expansion working, especially drove under the situation of recompression in the mechanical energy of utilizing expansion working to produce.At this moment, can unite and use turbine and supercharger, make expansion turbine and recompression machine reach mechanically combining by a common axis.
The 3rd feed air stream can be compressed to first pressure, and purifies with first, second feed air stream.It can directly recompress then, perhaps still recompresses with first feed air stream.
Perhaps, for the 3rd feed air stream being injected lower pressure column, second feed air stream is in further compression back but before entering mixing column, carry out expansion working.Further compression will reach second pressure apparently higher than mixing column pressure.
The present invention also relates to equipment as claimed in claim 9.
With reference to accompanying drawing, elaborate the present invention and further details thereof below with the embodiment of demonstrating.Herein:
Fig. 1 carries out the method and apparatus of expansion working when representing to be compressed to first pressure with the part air;
Fig. 2 carries out improving one's methods of expansion working when representing to be compressed to second pressure with the part air;
Fig. 3 represents to carry out with the mixing column air method of expansion working;
The another kind of improvement project of Fig. 4 presentation graphs 1, promptly the turbine air does not recompress.
In method shown in Figure 1, feeding air 1 is sent into two sections cold air compressors 2 of band back, is compressed to first pressure P 1, for example about 2.7～3.7 crust, preferred about 3.2 crust; Enter purification facility 3 under this pressure, this facility preferably is made of a pair of molecular sieve adsorber.Total air stream 4 after the purification is divided into 3 tributaries 5,6,7.
First feed air stream 5 further is compressed to second pressure P in the first recompression machine 8 2, for example 4.4～7.0 crust preferably about 5.7 cling to; Flow into main heat exchanger 10 through aftercooler 9 again.First feed air stream is left main heat exchanger 10 by pipeline 11 under dew-point temperature; Send into high-pressure tower 13 through pipeline 12.The operating pressure P of high-pressure tower 13 HDSCan be for example 4.3～6.9 to cling to, preferred about 5.6 crust.In addition, this distillation system also has lower pressure column 14, and its operating pressure is at for example 1.3～1.7 crust, and preferred about 1.5 cling to.
Second feed air stream 6 is also in about first pressure P 1(line loss and the pressure that deduct washing facility fall) finally flows into mixing column through pipeline 15 down by main heat exchanger 10.Feed points is close to top at the bottom of the tower of mixing column 16.
The 3rd air stream 7 is in the second recompression machine 17, from first pressure P 1Recompress the 3rd pressure P 3, for example 3.8～5.6 crust preferably about 4.7 cling to; Send into the hot junction of main heat exchanger then through aftercooler 18, pipeline 19.But it only is cooled to medium temperature, just before the cold junction of main heat exchanger 10, extract out through pipeline 50, and in turbine 20 expansion working.Air 21 after the expansion injects lower pressure column 14.Recompression machine 17 and turbine 20 are direct mechanically combinings.
In the embodiment of demonstration, distillation system is designed to classical Linde double tower facility, and it has condensation-evaporimeter 22 as main condenser.But the present invention also can use the distillation system of other condenser and/or tower structure.
The stream of oxygen-enriched liquid 23 of coming out from high-pressure tower 13 bottoms is crossed cooling in the cold contra-flow heat exchanger 24 at first, sends into lower pressure column 14 by choke valve 25 backs from middle position 26.The gaseous nitrogen 27 that comes out from high-pressure tower 13 tops, wherein a part 28 is heated in main heat exchanger 10, and as compressed nitrogen product 29 outputs; Remainder 30 is basic total condensation in main condenser 22.This place production fluid nitrogen 31, wherein at least a portion 32 is introduced high-pressure tower 13 as refluxing.If desired, another part 33 can be used as the liquid form product taking-up.Intermediate liquid stream 34 (the not purity nitrogens) of high-pressure tower are by can be used as the backflow of lower pressure column after subcooler 24 and the choke valve 35.From the gaseous state of lower pressure column cat head not purity nitrogen 36 be heated through heat exchanger 24 and 10, finally extract out through pipeline 37.As shown, it can be used as the regeneration gas of purification facility 3.
Liquid oxygen 38 is extracted out at the bottom of the low pressure Tata, reaches as 5.7～6.5 crust through pump 39 pressure, and preferred about 6.1 crust, heating in second cold contra-flow heat exchanger 40 of mistake then, final (41) introduce the top of mixing column 16.In second cold contra-flow heat exchanger 40 of mistake, overfire air stream 42 is cooled, this air stream is to tell from the first feed air stream upstream (upstream) that is in the main heat exchanger cold junction, or rather, is to extract out under the medium temperature that is lower than turbine 20 inlet temperatures.This air stream cools off after pipeline 43 converges with first feed air stream 11 again.By valve 44, can set the air fluxion amount of the cold contra-flow heat exchanger of second mistake of flowing through.The impure compressed oxygen 51 of gaseous state is extracted out from mixing column 16 tops, and the heating back is as product 52 outputs in main heat exchanger 10.Extract liquid 45 and tower middle part liquid 46 at the bottom of the tower out from mixing column, send into the suitable position of lower pressure column 14 respectively through pipeline 47 and 48.
Fig. 2 further compresses in first recompression machine 108 with second feed air stream with different the 3rd feed air stream 207 that only are of Fig. 1.As a result, reach higher inlet pressure, correspondingly the more colds of output at turbine 20.
In improvement project shown in Figure 3, purification facility is being higher than mixing column operating pressure P MiSFirst pressure P 1' operation down.First pressure P herein 1' be for example 2.7～3.7 to cling to, preferred about 3.2 crust.Second feed air stream 306 expands in the upstream that enters mixing column.There is not the 3rd feed air stream that enters lower pressure column.The further compression in the second recompression machine 317 after telling from the total air stream that purifies of second feed air stream 306, this compressor is driven by turbine 320.Further the pressure of compression back second feed air stream 349 for example is 3.8～5.6 crust, and preferred about 4.7 crust are sent into turbine 320 through pipeline 350, and expansion working reaches the mixing column pressure P approximately MiS
In the method for Fig. 4, be similar to the situation of Fig. 3, clean-up stage 3 is in the first low especially pressure P 1" operation down, for example 2.7～3.7 crust preferably about 3.2 cling to.Image pattern 1 is such, and turbine 420 is handled the 3rd feed air stream 407,450, but is not recompression herein, but the direct expansion work done, approximately from first pressure P 1" be reduced to about lower pressure column pressure.Recompression machine 418 is driven by turbine, further second feed air stream is compressed to second pressure P 2, this pressure is substantially equal to the operating pressure P of mixing column MiS
In all exemplary embodiment, air compressor and recompression machine 8,108 preferably have three sections co-ordinative constructions that compressor is such.In other words, the further compression that is equivalent to first feed air stream is that the 3rd section at compressor carries out, and first, second section then is used to compress the air of purification facility 3 upstreams.In addition, compressor also can be 4 sections, and in this case, first three section is arranged in before the purification facility 3.

Claims (9)

1, a kind of in the distillation system that comprises high-pressure tower (13) and lower pressure column (14), separate the method for producing compressed products by air low temperature, wherein:
First feed air stream (12) is introduced into high-pressure tower (13);
Oxygen enrichment cut (38) from lower pressure column (14) pressurizes under liquid state by (39), introduces mixing column (16) by (41) again;
Second feed air stream (6,15,306,406) is introduced into the Lower Half of mixing column (16), and carries out counter current contacting with oxygen enrichment cut (41);
Mixing column (16) operating pressure (P MiS) be lower than the operating pressure (P of high-pressure tower (13) HDS); And
Take out gaseous overhead product (51) from mixing column (16) first half, and as compressed products (52) output; It is characterized in that:
The total air stream (1) that contains first and second feed air stream is compressed to through (2) and is lower than high-pressure tower (13) operating pressure (P HDS) the first pressure (P 1), and greatly about this first pressure (P 1) under purify (3);
Total air stream (4) after the purification is divided into first (5) and second (6,306,406) feed air stream; And
First feed air stream (5) of separating with second feed air stream further compression (8,108) to the second pressure (P 2), this pressure equals the operating pressure (P of high-pressure tower (13) at least HDS).
2, the method for claim 1 is characterized in that, the first pressure (P 1) approximate the operating pressure (P of mixing column (16) greatly MiS).
3, the method for claim 1 is characterized in that first pressure is lower than the operating pressure (P of mixing column (16) MiS); Second feed air stream (306,406) of separating with first feed air stream further compression (317,417) to the 3rd pressure (P 3), this pressure equals the operating pressure (P of mixing column (16) at least MiS).
As the described method of one of claim 1～3, it is characterized in that 4, liquid oxygen enrichment cut with pressure is introduced mixing column (16) before in (41), make it heating by carrying out indirect heat exchanger (40) with overfire air stream (42).
As the described method of one of claim 1～4, it is characterized in that 5, the 3rd feed air stream (7,50,207,407,450) is through expansion working (20,420), and warp (21) is introduced lower pressure column (14).
As the described method of one of claim 1～5, it is characterized in that 6, the 3rd feed air stream (7) is recompressed (17) before at expansion working (20), and the mechanical energy that expansion working (20) is produced is used to recompress (17).
7, as the described method of one of claim 1～6, it is characterized in that, the 3rd feed air stream is to be made of a part that purifies the total air stream in back (4), and (7,207) directly send to recompression (17), sends to recompression (17) after perhaps uniting recompression (108) with first feed air stream.
As the described method of one of claim 1～4, it is characterized in that 8, second feed air stream (306,349,350) is expansion working (320) before introducing mixing column.
9, a kind of in the distillation system that comprises high-pressure tower (13) and lower pressure column (14), separate the equipment of producing compressed products by air low temperature, comprising:
The first feed air stream pipeline (5,11,12) that leads to high-pressure tower (13);
The oxygen enrichment cut is taken out and lead to the liquid line (38,41) of mixing column (16) from lower pressure column (14), comprise the equipment of boosting (39);
The second feed air stream pipeline (6,15) that leads to mixing column (16) Lower Half; And
Be connected to the oxygen product pipeline of mixing column (16) first half; It is characterized in that:
Total air flow tube line, this pipeline links to each other with the first and second feed air stream pipelines in the downstream through air compressor (2) and purification facility (3); And
Be arranged at the recompression machine (8,108) on the first feed air stream pipeline (5,11,12).
CNB01109513XA 2000-03-29 2001-03-28 Method and apparatus for low-temp. separation of air to produce compressed products Expired - Fee Related CN1179181C (en)

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ES2219230T3 (en) 2004-12-01
CN1179181C (en) 2004-12-08
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US20010052244A1 (en) 2001-12-20

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