CN106931721A - The method and air separation equipment of low temperature air separating - Google Patents
The method and air separation equipment of low temperature air separating Download PDFInfo
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- CN106931721A CN106931721A CN201611273154.3A CN201611273154A CN106931721A CN 106931721 A CN106931721 A CN 106931721A CN 201611273154 A CN201611273154 A CN 201611273154A CN 106931721 A CN106931721 A CN 106931721A
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- air
- supercharger
- pressure
- temperature
- tower
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- 238000000034 method Methods 0.000 title claims abstract description 80
- 238000000926 separation method Methods 0.000 title claims abstract description 44
- 238000004821 distillation Methods 0.000 claims abstract description 26
- 230000008569 process Effects 0.000 claims description 30
- 239000007788 liquid Substances 0.000 claims description 29
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 24
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 23
- 239000001301 oxygen Substances 0.000 claims description 23
- 229910052760 oxygen Inorganic materials 0.000 claims description 23
- 230000006837 decompression Effects 0.000 claims description 14
- 229910052757 nitrogen Inorganic materials 0.000 claims description 12
- 238000001816 cooling Methods 0.000 claims description 9
- 238000001704 evaporation Methods 0.000 claims description 5
- 230000008020 evaporation Effects 0.000 claims description 5
- 238000010438 heat treatment Methods 0.000 claims description 3
- 230000035611 feeding Effects 0.000 claims 7
- 239000000047 product Substances 0.000 description 32
- 238000007906 compression Methods 0.000 description 20
- 230000006835 compression Effects 0.000 description 20
- 239000007789 gas Substances 0.000 description 9
- 230000008901 benefit Effects 0.000 description 8
- 238000006243 chemical reaction Methods 0.000 description 8
- 230000008859 change Effects 0.000 description 6
- 238000000746 purification Methods 0.000 description 5
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 4
- 230000002411 adverse Effects 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 239000002826 coolant Substances 0.000 description 3
- 230000002349 favourable effect Effects 0.000 description 3
- 239000012263 liquid product Substances 0.000 description 3
- 238000005096 rolling process Methods 0.000 description 3
- 238000012546 transfer Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 2
- 238000004581 coalescence Methods 0.000 description 2
- 238000013461 design Methods 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000010521 absorption reaction Methods 0.000 description 1
- 230000003044 adaptive effect Effects 0.000 description 1
- 238000004458 analytical method Methods 0.000 description 1
- 229910052786 argon Inorganic materials 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 238000007664 blowing Methods 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000002828 fuel tank Substances 0.000 description 1
- 230000006870 function Effects 0.000 description 1
- 230000008676 import Effects 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 230000008450 motivation Effects 0.000 description 1
- 238000005457 optimization Methods 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 230000008929 regeneration Effects 0.000 description 1
- 238000011069 regeneration method Methods 0.000 description 1
- 238000007789 sealing Methods 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 238000009987 spinning Methods 0.000 description 1
- 238000004781 supercooling Methods 0.000 description 1
- 230000007704 transition Effects 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
- 230000003245 working effect Effects 0.000 description 1
Classifications
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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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/04054—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of air
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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
- F25J3/04078—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04175—Hot end purification of the feed air by adsorption of the impurities at a pressure of substantially more than the highest pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04375—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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- 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
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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
- F25J3/04763—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
- F25J3/04793—Rectification, e.g. columns; Reboiler-condenser
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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
- F25J3/04763—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
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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
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
- F25J2205/04—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum in the feed line, i.e. upstream of the fractionation step
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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- 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
- 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
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The method that the application suggestion utilizes air separation equipment (100) low temperature air separating with distillation column system (10), the distillation column system is included in the high-pressure tower (11) and the lower pressure column (12) in the work of lower pressure column stress level of high-pressure tower stress level work.The invention further relates to corresponding air separation equipment (100).
Description
Technical field
Air the present invention relates to the method for the low temperature air separating in air separation equipment and for implementing such method
Separation equipment.
Background technology
By the low temperature air separating in air separation equipment produce liquid or gaseous air products be it is known, for example
In H.-W.(Hrsg.), especially in Industrial Gases Processing, Wiley-VCH, 2006
2.2.5 section " Cryogenic Rectification (cryogenic rectification) " is described.
The air-separating plant with so-called interior compression is needed to use for a series of industrialized utilization gaseous state oxygen.
Corresponding air-separating plant is same to be illustrated in above-mentioned quotation and may be referred to its accompanying drawing 2.3A.Separated in corresponding air
Pressure is applied to super-low liquid, the liquid oxygen being especially under ultralow temperature in equipment, with respect to heat conduction evacuator body, is finally obtained
Gaseous product.Interior compression has the advantage in terms of energy conversion compared with additional compression is carried out to the gaseous product in low pressure.
Above-mentioned content is corresponding for other other products, such as again may be by gaseous state for nitrogen or argon gas
Under interior compression obtain and in advance as cryogenic liquid from distillation column system discharge.If corresponding cryogenic liquid is subject to exceed facing
The pressure of boundary's pressure, will not occur the evaporation on ordinary meaning, but change to supercriticality.This is referred to as " puppet evaporation ".
The interior compressed oxygen for being equally cryogenic liquid product can be by so-called High-Air-Pressure (HAP-) sides
Method is realized." cryogenic liquid product " can be understood as corresponding air separation equipment and can only carry a small amount of liquid product of discharge herein
Product, such as less than the 2% of all air capacities for importing Distallation systm.
HAP methods are construed as a kind of air separating method, wherein import Distallation systm all air (here also by
Certain pressure referred to as " air raw material ") is compressed into primary air discharge chambe first, the pressure is significantly greater than Distallation systm
In maximum working pressure (MWP).Air is particularly compressed to certain pressure first in HAP methods, in the pressure ratio Distallation systm
Operating pressure at least 4 to 5 bars high, most 20 bars high.In traditional double tower system with high-pressure tower and lower pressure column, destilling tower system
" maximum working pressure (MWP) " in system is the operating pressure of high-pressure tower.The cost of investment of the air separation equipment of HAP methods is particularly low,
Because needing only to a compressor.
In order to optimize HAP methods in terms of energy, it is possible to use so-called throttling stream.As known in principle, such throttling
Stream be compression feeding air tributary, its can continue boosting, cooling and via decompressor particularly choke valve depressurize into
In entering distillation column system or its high-pressure tower.
In the HAP methods, what such throttling stream can be applied by all feeding airs has been initial pressure high
Start, continue to boost by heat and cold supercharger.Air feeding is corresponding " supercharger of heat ", without or only than
Relatively low cooling is subsequent, such as in the water cooler in main air compressor downstream.The feeding end temperature of such hot supercharger is therefore
Apparently higher than 0 DEG C.The feeding temperature of " cold supercharger " is significantly low because the air before to importing cold supercharger is cooled down
In 0 DEG C.
Most of HAP methods have favourable Q/T features in main heat exchanger, when the oxygen pressure produced by interior compression
When power is more than 25 bar, it means that certain stress level is compressed under ultralow temperature and liquid condition by corresponding turbine.
When the pressure needed for interior compressed oxygen is dropped to significantly lower than 25 bar, the energy conversion efficiency of Q/T characteristics for HAP methods
It is relatively blunt.When pressure is in 6 to 25 bar, the conventional method with main compressor and auxiliary compressor seems more favourable.
In the method for being referred to as MAC/BAC methods (Main Air Compressor/Booster Air Compressor)
In, the partial air for sending into Distallation systm is only compressed into maximum working pressure (MWP) in Distallation systm or optionally smaller, and
Another air is compressed to pressure higher by auxiliary compressor.Such method is not being produced or is only producing minimal amount of liquid
It is particularly favourable during air products, such as liquid oxygen.If being produced for the gaseous air rich in nitrogen in such cases in addition
The demand of product is small, then particularly propose MAC/BAC methods, wherein entering to blow turbine using so-called, that is, the air decompression compressed is sent
Enter the turbine in the lower pressure column of distillation column system.
But, with HAP methods conversely, because the cost of compression set is higher, its investment cost is more for corresponding MAC/BAC methods
It is high.Therefore a kind of method is needed, it can have the low-cost advantage of HAP methods and especially into the MAC/BAC methods for blowing turbine
Above-mentioned advantage combine.
The content of the invention
Advise a kind of method for the low temperature air separating in air separation equipment under such background, and implement this
The air separation equipment of class method.Preferred embodiment is described below.
The application characterizes pressure and temperature using term " stress level " and " temperature levels ", thus expresses corresponding
Pressure and temperature need not be used in the form of accurate pressure value or temperature value in equipment, to realize the solution of the present invention.But
Such pressure and temperature generally in certain scope fluctuate, for example around intermediate value fluctuation ± 1%, 5%, 10%, 20% or
Even 50%.Here, corresponding stress level and temperature levels can be in discontinuous scope or in overlapped models
In enclosing.For example stress level especially includes the inevitable pressure loss or the expected pressure loss, and it is for example due to cooling
Effect or transmission loss cause.It is also applied for temperature levels accordingly.The stress level for being given with bar herein is related to absolute pressure.
It is used for compressed air using turbo-compressor in air separation equipment.Such as " main air compressor ", its feature
It is to be compressed all air of distillation column system, i.e., all air raw materials are imported by it.Accordingly can also be by
" auxiliary compressor " is set to turbo-compressor, is wherein compressed to the partial air in importing main compressor in MAC/BAC methods
Pressure higher.Other turbo-compressor are commonly designed in order to be compressed to partial air, in order to be carried out to partial air
Compression is commonly designed other turbo-compressor, and they are also referred to as supercharger, compared with main air compressor or auxiliary compressor,
It is only compressed in relatively small scope.
Air can be depressurized in addition on many positions of air separation equipment, wherein can be expanded using turbine
The negative booster of device form, wherein being also referred to as " turbine ".Turbine expander can also be connected simultaneously with turbo-compressor or supercharger
It is driven.When one or more turbo-compressor are not by external energy, i.e., only by one or more turbine pressures
When contracting machine is driven, such arrangement can also be referred to as " turbocharger ".Turbine expander and whirlpool in turbocharger
Wheel compression machine or supercharger are mechanically connected.
Rotary unit, such as negative booster or decompression turbine, compressor or compression stage, boosting turbine or supercharging can generally be made
The rotor of mechanical, electrical motivation or similar device are mechanically connected to each other in an appropriate manner.In " mechanical connection " linguistic context herein
It is understood to by mechanical part, such as similar device such as gear, belt, speed changer is realized fixing between these rotary parts
Or mechanical adjustable rotation speed relation.Mechanically connect and generally each intermeshed by two or more, for example, engaged with shape
Or the part of friction engagement, such as gear or belt pulley are realized using belt or the connected mode of other rotations.Rotation fixation
Connection particularly can be by common axle realization, the installation rotary unit that each spinning is fixed thereon.Rotary unit turn
Speed is in such cases identical.
Corresponding unit " mechanically decoupled ", refers between corresponding component in the absence of fixed or mechanical adjustable in contrast
Rotation speed relation.Can certainly be for example between multiple motor especially by suitable Electronic Control, or in multiple whirlpools
Between wheel specific rotation speed relation is preset especially by the suitable feeding of selection and terminal pressure.But this is not by one
Or multiple is each intermeshed, for example, realized with shape engagement or the part of friction engagement or the connection by rotating fixation.
The mechanical structure of turbo-compressor and turbine expander is known to professional person.In turbo-compressor by turn
Blades implement the compression of air, and the blade is disposed in rotor or is directly arranged on axle.Turbo-compressor is formed herein
Construction unit, but it has multiple " compression stages ".Compression stage generally includes rotor or corresponding rotor blade device.All pressures
Contracting level can be driven by same axis.Turbine expander is actually designed to what is referred to, but rotor blade here leads to
The air for crossing expansion is driven.Here multiple expansion stages are directed to.Turbo-compressor and turbine expansion can be designed to footpath
To or axial machine.
What is discussed in the category of the application is to obtain air products, particularly oxygen or nitrogen product." product " leaves
Described equipment and for example it is arranged in fuel tank or uses wherein.Therefore here not exclusively to the circulation of device interior,
Can also be used before equipment is left, such as the cooling agent in heat exchanger.The term of " product " does not therefore include
Such distillate or stream, themselves are stored in a device and only there as backflow, cooling agent or purge gas
Use.
Invention advantage
The present invention based on the recognition that, using the supercharger of arranged in series, the air to be compressed of the stream that throttles is its it
Between do not cooled down, can make HAP methods have the advantages that common MAC/BAC methods especially efficiently or at least in terms of energy conversion.
The heat exchange of heat exchange effect and usual method in the main heat exchanger in air separation equipment of the invention
Effect is compared more favorably, wherein implementing cooling during rolling between cold supercharger in usual way.In addition the present invention is based on
Hereinafter recognize, it is particularly advantageous using hot supercharger in the upstream of cold supercharger.Total of three supercharger can be pressed repeatedly herein
Casing coupling stream stream, but other streams are not compressed.On the one hand between heat exchanger, on the other hand in the supercharging of arranged in series
Particularly cooled down in main heat exchanger between machine and in the downstream of cold supercharger.
It is proposed that a kind of method for utilizing air separation equipment for low temperature air separating, it has destilling tower system
System, is included in the high-pressure tower and the lower pressure column in the work of lower pressure column stress level of the work of high-pressure tower stress level.High pressure pressure tower
Level is for example between 4 to 7 bars, i.e., generally horizontal in corresponding air separation equipment.Lower pressure column stress level is a little higher than big
Atmospheric pressure, particularly 1.2 to 1.8 bars, so as to for example ensure separative efficiency very high simultaneously on the premise of extra pump is not used
Derive the air products for entering lower pressure column.
HAP methods of the invention are comprised the following steps first, first by the air pressure in all feeding distillation column systems
It is reduced to the initial pressure level of up to fewer by 4 than high pressure pressure tower and most 20 bars.Used in the special scope of the invention
Air used is compressed to the stress level of 10 to 23 bars in main air compressor.Can also be filtered by molecule in the stress level
Net is dried and purifies to compressed air.
A part is compressed into initial pressure level and the air accordingly by drying and purifying is subsequent more than 0 DEG C
First temperature levels implement the first boost process, then implement two other liters in the temperature levels less than the first temperature levels
Press through journey.The air for implementing the first boost process can particularly set after the first boost process in respective air separation herein
Cooled down in standby main heat exchanger.Therefore corresponding air is pressed through in other liter of correspondingly lower temperature level implementation
Journey.
The air for implementing two other boost process then depressurizes into high-pressure tower.Section is used in order to carry out decompression
Stream valve.Therefore the referred to as so-called " throttling of air of two other boost process and the first boost process before is implemented
Stream ", the term is widely known in air separation field.
The oxygen enriched liquid of low temperature is discharged from lower pressure column, implements to boost in low-temperature condition, be subsequently heated and evaporate, from air point
Derived as air products from equipment.Therefore the method according to the invention is air separating method, wherein to oxygen or corresponding
Oxygen-enriched air product implements so-called internal compression.
According to the present invention, the first supercharger (i.e. " heat " supercharger, such as repeatedly mentions above) is pressed through for first liter
Journey, wherein the first supercharger is driven using the first negative booster, makes another part be compressed into initial pressure level wherein
Air be decompressed to second pressure level from initial pressure level, be subsequently sent in lower pressure column.Other parts are special at it
Before cooled down.First negative booster is so-called " injection turbine " or " La Heman turbines " according to its function, and it is in air point
Similarly it is widely known by the people from field.Can improve energy efficiency by the way that air is sprayed into lower pressure column accordingly.Detail can be with
With reference to technical literature, such as F.G.Kerry, Industrial Gas Handbook GasSeparation and
Purification, CRC Press, particularly 2006, chapters and sections 3.8.1, " The Lachmann Principle ".
Further according to the present invention, by the second supercharger and the 3rd supercharger (i.e. two " cold " superchargers) be used for two its
His boost process, one after the other directs air through wherein to implement two other boost process, and wherein air is leaving the
Temperature levels during two superchargers send into the 3rd supercharger.In other words do not enter between cold supercharger in scope of the invention
Row cooling during rolling, as according to knowable to the present invention, can realize more compared with usual way in the heat exchanger for being used
Good heat exchange effect.
Guiding is each amounted to by the first supercharger, the second supercharger and the 3rd supercharger and optionally by choke valve
According to the present invention, difference is no more than 10% to air capacity each other.Particularly these air capacities difference is no more than 5% or basic or complete
It is exactly the same.In other words, each experience first and two air capacities of additional boost process and optional decompression in choke valve
Air capacity it is similar or identical in mentioned scope.
It means that the first supercharger, the second supercharger and the 3rd supercharger and the pressure-reducing valve for optionally employing only are used
Stream in throttling stream, rather than the other air parts of offer or feeding distillation column system are provided.If from lower pressure column row
The low temperature oxygen enriched liquid for going out boosts to 6 to 25 bars with low-temperature condition, then advantages of the present invention is especially notable.According to it is of the present invention because
This devises corresponding pressure rise process.As stated in the beginning, generally in the pressure limit of the oxygen product of interior compression, tradition
MAC/BAC methods conversion efficiency than advantageous.But what the present invention using described in was connected does not carry out intercooled
Supercharger can also realize corresponding advantage in HAP methods.
If as described above, liquid production amount is small, i.e., based on the air capacity in all feeding distillation column systems, being separated from air
Equipment is with the air products that liquid derived proportions is most 1% or 0%, then of the invention particularly advantageous.Therefore entered according to the present invention
Above-mentioned design is gone.In addition the nitrogen-rich air product of relatively small amount is produced.Nitrogen-rich air product is the high pressure in distillation column system
Tower is discharged near top or top and is no longer back to high-pressure tower or lower pressure column.Therefore, particularly in scope of the invention,
Based on the air capacity in all feeding distillation column systems, the nitrogen-rich air product that ratio is most 2% is discharged simultaneously from high-pressure tower
Derived with gaseous state from air separation equipment.
The second supercharger and the 3rd supercharger each advantageously are driven by negative booster in scope of the invention, wherein
Another part after making to pre-cool and then depressurized in the negative booster in feeding distillation column system is compressed into initially
The air of stress level is depressurized.In order to drive the second supercharger used here as the second negative booster, in order to drive the 3rd supercharging
Machine uses the 3rd negative booster.It is different from the supercharger for two tandem workings of other boost process designs, corresponding decompression
Machine parallel connection (abreast) arrangement, it means that the air for driving negative booster is divided into two tributaries in advance.In this way can be with
Make decompression air capacity be respectively adaptive to needed for to negative booster be connected corresponding cold supercharger in pressure rise process or
In turn.
It is special that cold supercharger is driven by suitable mechanical connection by each negative booster.Corresponding mechanical connection can be with
With reference to content above.Actually corresponding supercharger can also be driven by motor, but from cost of investment and be passed to accordingly setting
Heat angle in standby set out be driven by corresponding negative booster it is particularly advantageous.
Air is advantageously set to be decompressed to high-pressure tower press water in the negative booster of the second supercharger and the 3rd supercharger is driven
It is flat.The partial liquefaction of air can be realized by corresponding decompression.Gaseous parts can be sent directly into high-pressure tower herein, and liquid
The part reduced pressure of change enters in lower pressure column.Liquefied part can in this way be back to lower pressure column and improve there and separate
Efficiency, such as, in the document chapters and sections 2.6 of Kerry, carry in " Theoretical Analysis of the Claude Cycle "
And.
The present invention allows further optimization and improves.The sky of initial pressure level can be particularly compressed into a part
Gas is cooled down, and since initial pressure level, i.e., the situation of additional boost is not being carried out by supercharger or similar device
Under, decompression enters in high-pressure tower.This can particularly be realized by other pressure-reducing valves.
Sending into the air in the second supercharger can particularly be cooled to the temperature of 130 to 200K in main heat exchanger in advance
Degree level.The air depressurized in the negative booster for driving the second supercharger and the 3rd supercharger be particularly be previously cooled to 120 to
The temperature levels of 190K.Drive the first supercharger the first negative booster in depressurize air be particularly be previously cooled to 150 to
The temperature levels of 230K.The air boosted in the 3rd supercharger is advantageously to subtract after this is boosted and at it
It was pressed into before in high-pressure tower and is cooled to the temperature levels of 97 to 105K, i.e. minimum temperature level, this can be by corresponding main
Heat exchanger is realized.Advantageously make the bar of pressure rise 10 to 25 by the second supercharger, pressure is advantageously made by the 3rd supercharger
Power raises 5 to 20 bars.
The air separation equipment with distillation column system the invention further relates to be used for low temperature air separating, the destilling tower system
System is included in the high-pressure tower and the lower pressure column in the work of lower pressure column stress level of high-pressure tower stress level work.
The air separation equipment includes being designed to herein the device of following purpose, first by all feeding destilling towers
Air in system is compressed to the initial pressure level of higher than high-pressure tower stress level at least 4 and most 20 bars；A part is pressed
The air for being reduced to initial pressure level implements the first boost process in the first temperature levels more than 0 DEG C, then less than first
The temperature levels of temperature levels implement two other boost process, followed by choke valve decompression feeding high-pressure tower；From low
Pressure tower discharges the oxygen enriched liquid of low temperature, and it implements to boost in low-temperature condition, is subsequently heated and evaporates, and is led from air separation equipment
Go out.The first supercharger is provided for the first temperature-rise period according to the present invention, it is mechanically coupled with the first negative booster, is provided with
For the device of following purpose, another part is set to be compressed into the air of initial pressure level in the first negative booster from initial pressure
Power level is decompressed to lower pressure column stress level, is subsequently sent in lower pressure column.According to the present invention for two other boost process
Second supercharger and the 3rd supercharger are provided, and are provided with the device for following purpose, pressed through for two other liters
Journey one after the other directs air through the second supercharger and the 3rd supercharger, the temperature water when this air is to leave the second supercharger
The 3rd supercharger of flat feeding.The device for following purpose is provided with, guiding is each amounted to by the first supercharger, the second supercharging
The air capacity of machine and the 3rd supercharger is differed no more than 10% each other.In addition the device for following purpose is provided with, from low pressure
The oxygen enriched liquid of the low temperature of tower discharge is set in the boost process that low-temperature condition is implemented in the form of boosting to 6 to 25 bars.
It is based in all feeding distillation column systems that the air separation equipment is designed to provide ratio with liquid
The air products of air capacity most 1%, it is based on all feeding distillations advantageously to be discharged from high-pressure tower and provide ratio with gaseous state
The nitrogen-rich air product of the air capacity most 2% in Tower System.
Such air separation equipment is particularly designed to implement the above method.Therefore may be referred to corresponding feature and
Advantage.
The present invention is expanded on further hereinafter with reference to appended diagram, and will illustrate specific thin by the structure type invented
Section.
Brief description of the drawings
Fig. 1 shows the air separation equipment of structure type of the invention with schematic flow sheet.
Fig. 2 is shown with the Q/T charts of the heat exchanger of structure type of the invention.
Fig. 3 is shown with the Q/T charts of the heat exchanger of structure type of the invention.
Specific embodiment
Fig. 1 shows a kind of air separation equipment of particularly advantageous structure type of the invention simultaneously with schematic flow sheet
Represented with 100.
Air separation equipment 100 sends into compressed air stream a, including primary air compression by air compression and purification unit 1
Machine and suitable purification system, wherein only rough illustrate.Air separation equipment shown in Fig. 1 is designed to so-called HAP
Method.It means that the stress level that compressed air stream a is compressed at least than the high-pressure tower 11 of distillation column system 10 is high by 4 to 20
The stress level of bar, compressed air stream includes all air of the distillation column system 10 of feeding air separation equipment 100.
The stress level for flowing a is known as " initial pressure level " herein, and the stress level of high-pressure tower 11 is referred to as " high pressure
Pressure tower level ".4 tributaries of generation are had altogether from compressed air stream a, in initial pressure level wherein being represented with b, c, d and e.
The air of tributary b is boosted in supercharger 2 first herein.Boosting in supercharger 2 is referred to herein as
" the first boost process ", its temperature more than 0 DEG C is carried out, therefore supercharger 2 is also generally referred to as " hot supercharger ".
The air of tributary b is then sent into empty by being cooled down in aftercooler 3 after the boosting in supercharger 2 in hot side
The main heat exchanger 4 of gas separation equipment 100.The air of tributary b is from main heat exchanger 4 (referring to connection A) with significantly lower than 0 DEG C
Medium temperature level is discharged.The air correspondingly through cooling down of tributary b is with latter two other boost process.It is this tributary b's
Air by supercharger 5, then passes through supercharger 6 first.Supercharger 5 is referred to herein as " second ", and supercharger 6 is also claimed
It is " the 3rd " supercharger.Two superchargers 5,6 in the temperature levels significantly lower than 0 DEG C, particularly in first less than supercharger 2
The temperature levels work of temperature levels.Therefore they are also referred to as " cold supercharger ".
The temperature levels when air of tributary b leaves the second supercharger 5 with it send into the 3rd supercharger 6.In the second supercharging
Cooling during rolling is not carried out between the supercharger 6 of machine 5 and the 3rd.After boosting in supercharger 6, the air of tributary b is left with it
Temperature levels during three superchargers 6 are re-fed into main heat exchanger 4 and in cold side discharge.
Supercharger 5 and 6 is driven by negative booster 7 and 8, and wherein using the air of tributary c, it is divided into tributary f and g for this.
The air of tributary c is first fed into the hot side of main heat exchanger and is discharged in medium temperature level herein, before this it
In being divided into mentioned tributary f and g and sending into negative booster 7,8.
The air of tributary d is sent into the hot side of main heat exchanger 4 and is discharged in cold side, and the air of tributary e sends into main heat
The hot side of exchanger 4, is discharged and in negative booster 9 for driving supercharger 2 in medium temperature level.
The reduced pressure air of tributary f and g is converted in separator 13, wherein isolating liquid phase.Liquid phase (referring to connection B)
Entered in lower pressure column 12 with being depressurized in the form of flowing h.The air for still keeping gaseous part for flowing f and g sends into height in the form of flowing i
In pressure tower 11.The air of tributary b and d is depressurized by valve 14 and 15 and entered in high-pressure tower 11.In the feeding mouth for flowing b and d just
Lower section can obtain flowing the liquid part of q forms by depressurizing from high-pressure tower 11, guiding by being subcooled adverse current device 16, and with stream h
Decompression together enters in lower pressure column 12.
The gaseous state of liquid tower bottom product and the nitrogen enrichment of oxygen coalescence is formed using the air for flowing b, d and i in high-pressure tower 11
Overhead product.The liquid tower bottom product of oxygen coalescence is at least partly discharged in lower pressure column 11 in the form of flowing k, and guiding is by supercooling
Adverse current device 16, and depressurize into lower pressure column 12.Gaseous overhead product at least a portion of nitrogen enrichment is discharged in the form of flowing 1.
A portion can be heated in the form of m and as the pressure product of rich nitrogen from air using flowing in main heat exchanger 4
Exported in separation equipment 100, such as be used as dense gas in the main air compressor of air compression and purification unit 1
(sealing gas Dichtgas).
At least part of liquid in the main condenser 17 that another part of stream 1 can be connected with high-pressure tower and lower pressure column heat exchange
Change.Corresponding partial liquefaction product can be back to high-pressure tower 11, and another part is guided by the way that adverse current device is subcooled in the form of flowing n
16, and depressurize into lower pressure column 12.
Oxygen-enriched liquid tower bottom product and gaseous overhead product is formed in lower pressure column 12.The oxygen-enriched liquid of lower pressure column 12
State tower bottom product can be obtained from high-pressure tower 12 in the form of flowing o and be liquid by 18 liters of high pressure transitions of pump at least in part
State, heating and evaporation and the oxygen enriched product as interior compression are exported from air separation equipment 100 in main heat exchanger 4.
The gaseous overhead product of lower pressure column 12 can at least in part to flow as the discharge of so-called not purity nitrogen in the form of p,
Guiding is heated by the way that adverse current device 16 is subcooled in main heat exchanger 4, for example, be used as absorption in air compression and purification unit 1
The regeneration gas of device.
The workflow of the air separation equipment 100 shown by Fig. 1 can be realized particularly advantageous in main heat exchanger 4
Heat exchange, on condition that meeting above-mentioned other conditions.This is by by the Q/T chart explanations shown in Fig. 2 and 3.
Show corresponding Q/T charts in fig. 2, the oxygen-enriched air for flowing o is compressed in the pump 18 of air separation equipment 100
To the stress level of about 15.0 bars, show that pressure is about the corresponding Q/T charts of 10.0 bars in figure 3.Here abscissa
The temperature in units of K is represented, ordinate represents the enthalpy (total amount) of the heat exchanger in units of MW.201 shapes for representing heat
State change curve or master curve, 202 represent the state change curve or master curve of cooling agent, wherein being stream o to be heated
Oxygen-enriched air.From Fig. 2 and 3 as can be seen that state change curve or master curve 201 and 202 are due to using of the invention
Respective air separation equipment curve is closely.
Hot and cold master curve in main heat exchanger closer to, because the energy conversion loss that heat transfer is caused is fewer, because
It is the energy conversion loss and 1/T caused by heat transfer2It is proportional, the temperature difference under the angle " low temperature " of energy conversion
It is particularly disadvantageous.T hereinbefore represents the temperature levels of local heat transfer.
Therefore as illustrated, when hot and cold master curve in the range of 200 to 100K, then it is worked in main heat exchanger
Journey is highly beneficial in the meaning or can in such cases improve the energy conversion efficiency of whole system.
Claims (13)
1. using the method for air separation equipment (100) low temperature air separating with distillation column system (10), the destilling tower system
System is included in the high-pressure tower (11) and the lower pressure column (12) in the work of lower pressure column stress level of high-pressure tower stress level work, wherein
The method includes：
- air in all feedings distillation column system (10) are compressed to higher than high-pressure tower stress level at least 4 and at most first
The initial pressure level of 20 bars,
The air a that-part is compressed into initial pressure level implements the first boost process in the first temperature levels more than 0 DEG C,
Then implement two other boost process in the temperature levels less than the first temperature levels, depressurized followed by choke valve (14)
In feeding high-pressure tower (11),
- from the oxygen enriched liquid of lower pressure column (12) discharge low temperature, the oxygen enriched liquid of the low temperature is implemented to boost in low-temperature condition, heating
And evaporation, derived from air separation equipment (100),
Characterized in that,
- the first supercharger (2) is used for the first boost process, it is driven using the first negative booster (9), is made wherein another
The air that a part is compressed into initial pressure level is decompressed to lower pressure column stress level from initial pressure level, is subsequently sent to low
In pressure tower (12),
- increased using the second supercharger (5) therein and the 3rd is one after the other directed air through for two other boost process
Press (6), wherein air send into the 3rd supercharger (6) to leave temperature levels during the second supercharger (5),
- respective total guides the air capacity for passing through the first supercharger (2), the second supercharger (5) and the 3rd supercharger (6) phase each other
Difference is no more than 10%,
- low temperature the oxygen enriched liquid from lower pressure column (12) discharge is to boost to 6 to 25 bars in the boost process that low-temperature condition is implemented,
- based on the air capacity in all feedings distillation column system (10), be with liquid derived proportions from air separation equipment (100)
Most 1% air products.
2. method according to claim 1, wherein based on the air capacities in all feedings distillation column system (10), by ratio for most
Many 2% nitrogen-rich air product is discharged from high-pressure tower (11) and derived with gaseous state from air separation equipment (100).
3. according to the method for claim 1 or 2, wherein the second supercharger (5) and the 3rd supercharger (6) are each by negative booster
(7,8) drive, the another part for pre-cooling and being subsequently sent in distillation column system (10) is compressed into initial pressure wherein
Depressurized the air parallel of power level.
4. method according to claim 3, wherein air are driving the negative booster of the second supercharger (5) and the 3rd supercharger (6)
Carry out being decompressed to high-pressure tower stress level in (7,8).
5. method according to claim 4, wherein air are by driving subtracting for the second supercharger (5) and the 3rd supercharger (6)
High-pressure tower stress level is decompressed in press (7,8) and partial liquefaction, wherein gaseous part will be kept to send into high-pressure tower (11)
In and liquefied part sent into lower pressure column (12).
6. according to the method for one of preceding claims, wherein cooling another part is compressed into the air of initial pressure level,
And depressurized into high-pressure tower (11) since initial pressure level.
7. according to the method for one of preceding claims, wherein the air that will be fed into the second supercharger (5) be previously cooled to 130 to
The temperature levels of 200K.
8. according to the method for one of claim 3 to 7, wherein driving the decompression of the second supercharger (5) and the 3rd supercharger (6)
The air of decompression was cooled to the temperature levels of 120 to 190K before its decompression in machine (7,8).
9. according to the method for one of preceding claims, wherein the air of the decompression in the first negative booster (9) is previously cooled to
The temperature levels of 150 to 230K.
10. according to the method for one of preceding claims, wherein by the air of the boosting in the 3rd supercharger (6) its depressurize into
The temperature levels of 97 to 105K are cooled to before entering in high-pressure tower (11).
11. according to the method for one of preceding claims, wherein the boost process in the second supercharger (5) is liter high pressure 10
To 25 bars, the boost process in the 3rd supercharger (6) is liter bar of high pressure 5 to 15.
12. air separation equipments (100) with distillation column system (10) for being used for low temperature air separating, the distillation column system bag
The high-pressure tower (11) and the lower pressure column (12) in the work of lower pressure column stress level in the work of high-pressure tower stress level are included, wherein described
Air separation equipment (100) is including being designed to the device of following purpose：
- air in all feedings distillation column system (10) are compressed to higher than high-pressure tower stress level at least 4 and at most first
The initial pressure level of 20 bars,
The air a that-part is compressed into initial pressure level implements the first boost process in the first temperature levels more than 0 DEG C,
Then implement two other boost process in the temperature levels less than the first temperature levels, depressurized followed by choke valve (14)
In feeding high-pressure tower (11),
- from the oxygen enriched liquid of lower pressure column (12) discharge low temperature, the oxygen enriched liquid of the low temperature is implemented to boost in low-temperature condition, then
Heating and evaporation, derive from air separation equipment (100),
Characterized in that,
- the first supercharger (2) is provided for the first temperature-rise period, it is mechanically coupled with the first negative booster (9), is provided with useful
In the device of following purpose, another part is set to be compressed into the air of initial pressure level in the first negative booster (9) from initial
Stress level is decompressed to lower pressure column stress level, is subsequently sent in lower pressure column (12),
- provide the second supercharger (5) and the 3rd supercharger (6) for two other boost process, and be provided with for
The device of lower purpose, the second supercharger (5) and the 3rd supercharging are one after the other directed air through for two other boost process
Machine (6), the temperature levels when this air is to leave the second supercharger (5) send into the 3rd supercharger (6),
- device for following purpose is provided with, guiding is each amounted to by the first supercharger (2), the second supercharger (5) and the
The air capacity of three superchargers (6) is differed no more than 10% each other,
- device for following purpose is provided with, implement in low-temperature condition from the low temperature oxygen enriched liquid of lower pressure column (12) discharge
Boost process is set in the form of boosting to 6 to 25 bars,
It is based in all feedings distillation column system (10) that-air separation equipment (100) is designed to provide ratio with liquid
Air capacity most 1% air products.
13. air separation equipments (100) according to claim 12, its be designed to implement according to claim 1 to 11 it
One method.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| EP15003482.5 | 2015-12-07 | ||
| EP15003482.5A EP3179185A1 (en) | 2015-12-07 | 2015-12-07 | Method for the low-temperature decomposition of air and air separation plant |
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| CN106931721A true CN106931721A (en) | 2017-07-07 |
| CN106931721B CN106931721B (en) | 2020-12-01 |
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| CN201611273154.3A Expired - Fee Related CN106931721B (en) | 2015-12-07 | 2016-12-06 | Method for the cryogenic separation of air and air separation plant |
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| Country | Link |
|---|---|
| EP (2) | EP3179185A1 (en) |
| CN (1) | CN106931721B (en) |
| RU (1) | RU2721195C2 (en) |
| TR (1) | TR201905990T4 (en) |
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| CN101421575A (en) * | 2006-03-15 | 2009-04-29 | 林德股份公司 | Method and apparatus for fractionating air at low temperatures |
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| RU2054609C1 (en) * | 1990-12-04 | 1996-02-20 | Балашихинское научно-производственное объединение криогенного машиностроения им.40-летия Октября "Криогенмаш" | Air separation method |
| FR2895068B1 (en) * | 2005-12-15 | 2014-01-31 | Air Liquide | AIR SEPARATION METHOD BY CRYOGENIC DISTILLATION |
| DE102007014643A1 (en) * | 2007-03-27 | 2007-09-20 | Linde Ag | Method for producing gaseous pressurized product by low temperature separation of air entails first and fourth partial air flows being expanded in turbines, and second and third partial flows compressed in post-compressors |
| FR3014545B1 (en) * | 2013-12-05 | 2018-12-07 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
| EP3101374A3 (en) * | 2015-06-03 | 2017-01-18 | Linde Aktiengesellschaft | Method and installation for cryogenic decomposition of air |
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2015
- 2015-12-07 EP EP15003482.5A patent/EP3179185A1/en not_active Withdrawn
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2016
- 2016-11-24 TR TR2019/05990T patent/TR201905990T4/en unknown
- 2016-11-24 EP EP16020464.0A patent/EP3179188B1/en not_active Not-in-force
- 2016-12-06 RU RU2016147700A patent/RU2721195C2/en active
- 2016-12-06 CN CN201611273154.3A patent/CN106931721B/en not_active Expired - Fee Related
Patent Citations (5)
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| US5475980A (en) * | 1993-12-30 | 1995-12-19 | L'air Liquide, Societe Anonyme Pour L'etude L'exploitation Des Procedes Georges Claude | Process and installation for production of high pressure gaseous fluid |
| CN1890525A (en) * | 2003-12-10 | 2007-01-03 | 液体空气乔治洛德方法利用和研究的具有监督和管理委员会的有限公司 | Process and apparatus for the separation of air by cryogenic distillation |
| CN101421575A (en) * | 2006-03-15 | 2009-04-29 | 林德股份公司 | Method and apparatus for fractionating air at low temperatures |
| EP2520886A1 (en) * | 2011-05-05 | 2012-11-07 | Linde AG | Method and device for creating gaseous oxygen pressurised product by the cryogenic decomposition of air |
| CN104204699A (en) * | 2012-03-29 | 2014-12-10 | 乔治洛德方法研究和开发液化空气有限公司 | Process for the separation of air by cryogenic distillation |
Also Published As
| Publication number | Publication date |
|---|---|
| TR201905990T4 (en) | 2019-05-21 |
| EP3179188A1 (en) | 2017-06-14 |
| RU2016147700A3 (en) | 2020-03-05 |
| EP3179188B1 (en) | 2019-01-30 |
| EP3179185A1 (en) | 2017-06-14 |
| RU2721195C2 (en) | 2020-05-18 |
| RU2016147700A (en) | 2018-06-08 |
| CN106931721B (en) | 2020-12-01 |
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