CN108036584A - The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification - Google Patents
The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification Download PDFInfo
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- CN108036584A CN108036584A CN201711464387.6A CN201711464387A CN108036584A CN 108036584 A CN108036584 A CN 108036584A CN 201711464387 A CN201711464387 A CN 201711464387A CN 108036584 A CN108036584 A CN 108036584A
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- liquid
- oxygen
- nitrogen
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- destilling tower
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- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 title claims abstract description 196
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 title claims abstract description 129
- 239000001301 oxygen Substances 0.000 title claims abstract description 129
- 229910052760 oxygen Inorganic materials 0.000 title claims abstract description 129
- 229910052757 nitrogen Inorganic materials 0.000 title claims abstract description 98
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 title claims abstract description 42
- 238000000034 method Methods 0.000 title claims abstract description 20
- 239000007788 liquid Substances 0.000 claims description 132
- 238000004821 distillation Methods 0.000 claims description 43
- 239000002699 waste material Substances 0.000 claims description 39
- 206010058490 Hyperoxia Diseases 0.000 claims description 23
- 239000012530 fluid Substances 0.000 claims description 23
- 230000000222 hyperoxic effect Effects 0.000 claims description 23
- 238000009835 boiling Methods 0.000 claims description 21
- 238000001816 cooling Methods 0.000 claims description 19
- 239000007789 gas Substances 0.000 claims description 14
- 238000009833 condensation Methods 0.000 claims description 13
- 230000005494 condensation Effects 0.000 claims description 13
- 238000000746 purification Methods 0.000 claims description 7
- 230000006835 compression Effects 0.000 claims description 5
- 238000007906 compression Methods 0.000 claims description 5
- 238000009834 vaporization Methods 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 238000004891 communication Methods 0.000 claims description 3
- 238000000926 separation method Methods 0.000 claims description 2
- 238000004519 manufacturing process Methods 0.000 abstract description 5
- DOTMOQHOJINYBL-UHFFFAOYSA-N molecular nitrogen;molecular oxygen Chemical compound N#N.O=O DOTMOQHOJINYBL-UHFFFAOYSA-N 0.000 abstract description 3
- 238000005265 energy consumption Methods 0.000 abstract description 2
- XKRFYHLGVUSROY-UHFFFAOYSA-N Argon Chemical compound [Ar] XKRFYHLGVUSROY-UHFFFAOYSA-N 0.000 description 8
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 6
- 229910052786 argon Inorganic materials 0.000 description 4
- 238000010438 heat treatment Methods 0.000 description 4
- 239000012071 phase Substances 0.000 description 4
- 238000010792 warming Methods 0.000 description 4
- 239000001569 carbon dioxide Substances 0.000 description 3
- 229910002092 carbon dioxide Inorganic materials 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- 238000005516 engineering process Methods 0.000 description 2
- 239000012535 impurity Substances 0.000 description 2
- 239000007791 liquid phase Substances 0.000 description 2
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 2
- 239000002912 waste gas Substances 0.000 description 2
- 239000004215 Carbon black (E152) Substances 0.000 description 1
- 206010013786 Dry skin Diseases 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000003466 anti-cipated effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910052799 carbon Inorganic materials 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000000428 dust Substances 0.000 description 1
- 238000001704 evaporation Methods 0.000 description 1
- 230000008020 evaporation Effects 0.000 description 1
- 238000002309 gasification Methods 0.000 description 1
- 239000001307 helium Substances 0.000 description 1
- 229910052734 helium Inorganic materials 0.000 description 1
- SWQJXJOGLNCZEY-UHFFFAOYSA-N helium atom Chemical compound [He] SWQJXJOGLNCZEY-UHFFFAOYSA-N 0.000 description 1
- 229930195733 hydrocarbon Natural products 0.000 description 1
- 150000002430 hydrocarbons Chemical class 0.000 description 1
- 239000001257 hydrogen Substances 0.000 description 1
- 229910052739 hydrogen Inorganic materials 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 229910052743 krypton Inorganic materials 0.000 description 1
- DNNSSWSSYDEUBZ-UHFFFAOYSA-N krypton atom Chemical compound [Kr] DNNSSWSSYDEUBZ-UHFFFAOYSA-N 0.000 description 1
- 229910052754 neon Inorganic materials 0.000 description 1
- GKAOGPIIYCISHV-UHFFFAOYSA-N neon atom Chemical compound [Ne] GKAOGPIIYCISHV-UHFFFAOYSA-N 0.000 description 1
- 238000010926 purge Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
- 229910052724 xenon Inorganic materials 0.000 description 1
- FHNFHKCVQCLJFQ-UHFFFAOYSA-N xenon atom Chemical compound [Xe] FHNFHKCVQCLJFQ-UHFFFAOYSA-N 0.000 description 1
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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
- F25J3/04436—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 at least a triple pressure main column system
- F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
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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
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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
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
- F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
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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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
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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
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04612—Heat exchange integration with process streams, e.g. from the air gas consuming unit
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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
- F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
- F25J2200/94—Details relating to the withdrawal point
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/42—Nitrogen or special cases, e.g. multiple or low purity N2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/52—Oxygen production with multiple purity 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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
- F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/10—Boiler-condenser with superposed stages
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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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
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- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
The invention discloses a kind of method and apparatus for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification, can meet the needs of market is to nitrogen and oxygen at the same time, while yield is ensured, and can realize the requirement to nitrogen oxygen purity.The present invention has taken into full account each side factor to realize production High Purity Nitrogen, oxygen and steady, efficient, low energy consumption the operation of liquid oxygen plant.
Description
Technical field
The present invention relates to the method and apparatus that High Purity Nitrogen, oxygen and liquid oxygen are produced by cryogenic rectification.
Background technology
Mixture containing nitrogen and oxygen, most commonly air, rich nitrogen can be separated into through cryogenic rectification and oxygen-enriched is evaporated
Point and the cut comprising rare gas, such as argon gas.In cryogenic rectification, by air purge, compress, to remove height boiling impurity
(such as carbon dioxide), water vapour and hydrocarbon.Then the air stream of the purifying of gained and compression is cooled to suitable for essence
The temperature evaporated.The rich nitrogen of rectifying generation and oxygen-enriched cut and other desired cut, it can be liquids and gases Product Form.
There are different rectifying columns to arrange for this purpose.
In recent years, it is big to the demand of High Purity Nitrogen and high pure oxygen in fields such as petrochemical industry, blast furnace ironmaking, electronic industries
Big increase.Therefore efficient, energy saving, the production High Purity Nitrogen and the method and apparatus of high pure oxygen cut down expenses is needed.
Chinese utility model patent CN202648307U describes a kind of equipment that air is separated by cryogenic rectification, profit
High Purity Nitrogen can be produced in a destilling tower with two condensers for being arranged in tower top.But height can only be produced in the utility model
Purity nitrogen and high pure oxygen cannot be produced, can not meet the needs of for high pure oxygen, without general applicability.
The content of the invention
The technical problems to be solved by the invention are how on the premise of the production of High Purity Nitrogen is unaffected, and production is high-purity
High pure oxygen and oxygen are produced while nitrogen.
To solve the above-mentioned problems, disclose one kind and High Purity Nitrogen, oxygen and liquid oxygen are produced from air by cryogenic rectification
Method.Compressed the first raw air after purification is provided to the first distillation section of the first destilling tower first, and first
First raw air is separated into the first oxygen enriched liquid of the first nitrogen rich vapor and bottom of towe on top, the first rich nitrogen in destilling tower
Steam and the first oxygen enriched liquid all may be logically divided at least two parts, wherein the first nitrogen rich vapor of Part I and Part I first
Oxygen enriched liquid makes the condensation generation Part I richness nitrogen condensation of the first nitrogen rich vapor of Part I in the first condenser indirect heat exchange
Liquid, while at least a portion vaporization of the first oxygen enriched liquid, generate the second nitrogen rich vapor and hyperoxia quantity of fluid.It is alternatively possible to
The first nitrogen rich vapor of part is taken out as nitrogen product.
Then a part of hyperoxia quantity of fluid carries out indirect heat exchange with the first nitrogen rich vapor of Part II in the second condenser,
Make the first nitrogen rich vapor of Part II condensation generation Part II richness nitrogen condensate liquid, while at least a portion hyperoxia quantity of fluid vapour
Change, generate the first waste stream.At least partly above-mentioned rich nitrogen condensate liquid is returned into the first destilling tower as phegma, alternatively,
Portion's separation nitrogen-enriching condensate liquid can also be taken out as liquid nitrogen product.
By the second nitrogen rich vapor of part through the first compressor formed first circulation stream, after it is cold by the first main heat exchanger
But the after-fractionating section of the first destilling tower, and by the first circulation stream of cooling is conveyed into, wherein, after-fractionating section is positioned at the
The one at least one theoretical cam curve in distillation section lower section and interval.
From the second condenser, extract vaporization after remaining hyperoxia quantity of fluid, and as the second oxygen enriched liquid it is expanded after
It is sent into after-fractionating tower, the second oxygen enriched liquid after expansion includes the gentle body portion of liquid portion, and liquid portion flows downward
To the after-fractionating tower reboiler positioned at after-fractionating tower lower part, gas part rises and generates the second waste stream at top, should
After second waste flows through the second main heat exchanger re-heat heating, it can at least partly flow through generation second after the second compressor compresses and follow
Circulation, in the second main heat exchanger, second circulation stream and compressed the second raw air after purification, with high pressure liquid oxygen and
After second waste stream indirect heat exchange and cooling, after-fractionating tower lower space is inputted.
After-fractionating tower lower space contains oxygen deprivation steam and poor oxygen liquid, and a part of oxygen deprivation steam is conveyed as heat source
Enter after-fractionating tower reboiler, and indirect heat exchange, oxygen deprivation steam heat exchange rear portion are carried out with the second oxygen enriched liquid after rectifying
Divide condensation to generate poor oxygen liquid and return to after-fractionating tower lower space.
Remaining second liquid oxygen in after-fractionating tower reboiler is extracted, can be after liquid oxygen pump be pressurized, in the second main heat exchange
Exported in device after re-heat as the second oxygen product.
Poor oxygen liquid in after-fractionating tower lower space can at least be divided into two parts, and the poor oxygen liquid of Part I is expanded
Be introduced into after-fractionating tower upper space as phegma afterwards, the poor oxygen liquid of Part II can it is expanded after can be with the first oxygen-rich liquid
Body mixes and is admitted to the first condenser.
A part for phegma is extracted from the 3rd distillation section of the first destilling tower, the liquid air as no high boiling component passes through
Cross after expansion valve and be conveyed into the top of the 3rd destilling tower, wherein, the 3rd distillation zone section is above the first distillation section and is spaced
At least one theoretical cam curve.
The liquid air without high boiling component after expansion includes the gentle body portion of liquid portion, and liquid portion flows downward in place
In the 3rd destilling tower reboiler of the 3rd destilling tower lower space, with the first oxygen-rich liquid of Part II introduced from the first destilling tower
Body indirect heat exchange, and generate the 3rd liquid oxygen product, the first oxygen-rich liquid of Part II after cooling in the bottom of the 3rd destilling tower
Body is transmitted back to the first or second condenser.
The 3rd waste stream is generated in the upper space of the 3rd destilling tower, alternatively, after merging with the first waste stream, first
Main heat exchanger and compressed the first raw air indirect heat exchange after purification.Cold needed for cryogenic rectification process is by expanding
At least one of first waste stream and/or first raw air are expanded in machine to provide.Wherein the first compressor and swollen
Swollen machine is mechanical communication.
, should the invention also discloses a kind of equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification
Equipment includes：
The equipment that raw air is compressed, purifies and the logistics for generating itself and cryogenic rectification carry out indirect heat exchange with the
The first main heat exchanger that one destilling tower is connected and the second main heat exchanger being connected with after-fractionating tower.
Comprising some distillation sections, the first raw air of compressed, purifying, cooling is provided to the first distillation section, will
It is separated into the first destilling tower in first nitrogen rich vapor on top and the first oxygen enriched liquid of bottom of towe.
The first nitrogen rich vapor of Part I and the first oxygen enriched liquid of Part I is carried out indirect heat exchange, make Part I
First nitrogen rich vapor condensation generation Part I richness nitrogen condensate liquid, makes the first oxygen enriched liquid of Part I at least partly gasify, raw
Into the second nitrogen rich vapor and the first condenser of hyperoxia quantity of fluid.
At least part of hyperoxia quantity of fluid is carried out indirect heat exchange with the first nitrogen rich vapor of Part II, make Part II
First nitrogen rich vapor condensation generation Part II richness nitrogen condensate liquid, makes the hyperoxia quantity of fluid at least partly gasify, generation first
Second condenser of waste stream.
To send at least partly rich nitrogen condensate liquid equipment of first destilling tower as phegma back to.
To the first compressor for compressing the second nitrogen rich vapor, to cool down first circulation stream, and by first circulation stream
Send to the equipment of the after-fractionating section of the first destilling tower, wherein, after-fractionating section positioned at first distillation section below and
Every at least one theoretical cam curve.
Remaining hyperoxia quantity of fluid is as the expanded rear feeding second of the second oxygen enriched liquid after being vaporized in second condenser
The pipeline and expansion valve of destilling tower.
After-fractionating tower, after-fractionating tower upper space, after-fractionating tower distillation section, after-fractionating tower lower space and
For the after-fractionating tower reboiler of reboiling liquid oxygen.
The second main heat exchanger re-heat is inputted from after-fractionating tower upper space by the second waste stream, and through the second compressor
Defeated time the second main heat exchanger cooling, then input the pipeline of after-fractionating tower lower space again after compression.
Pressurized, purifying the second raw air is inputted into the cooling of the second main heat exchanger, then is inputted under after-fractionating tower
The pipeline in portion space.
Oxygen deprivation steam in after-fractionating tower lower space is conveyed into the pipeline of after-fractionating tower reboiler, and will condensation
Poor oxygen liquid afterwards is transmitted back to the pipeline of after-fractionating tower lower space.
The second main heat is conveyed into after the second liquid oxygen in after-fractionating tower reboiler is pressurized alternatively through liquid oxygen pump to hand over
Parallel operation re-heat, and as the pipeline of the second oxygen product output.
Poor oxygen liquid in after-fractionating tower lower space (43) is conveyed into the pipe of after-fractionating tower upper space respectively
Road and the pipeline converged with the first oxygen enriched liquid.
In the first destilling tower, in the 3rd distillation that first distills at least one theoretical cam curve in above section and interval
Section, a part for phegma is extracted from the 3rd distillation section, and the liquid air as no high boiling component conveys after expansion valve
Enter the equipment at the top of the 3rd destilling tower.
Positioned at the 3rd destilling tower reboiler of the 3rd destilling tower lower space, wherein, after expansion without high boiling component
Liquid portion in liquid air, flows through the distillation section of the 3rd destilling tower, herein the Part II with being introduced from the first destilling tower
One oxygen enriched liquid indirect heat exchange, and the 3rd liquid oxygen product is generated in the bottom of the 3rd destilling tower, Part II after cooling the
One oxygen enriched liquid is transmitted back to the first or second condenser.
The 3rd waste stream that will be generated at the top of the 3rd destilling tower, alternatively, after merging with the first waste stream, send to
The equipment of one main heat exchanger and the first raw air indirect heat exchange.
At least partly first waste stream and/or first raw air are expanded and provided for cryogenic rectification process
The expanding machine of required cold.
Wherein, first compressor and expanding machine are mechanically coupled.
Wherein, the first condenser, the second condenser and reboiler are made of plate heat exchanger in the said equipment.
Using the method and apparatus of production High Purity Nitrogen disclosed by the invention, oxygen and liquid oxygen, it can meet market pair at the same time
The demand of nitrogen and oxygen, while yield is ensured, and can realize the requirement to nitrogen oxygen purity.The present invention has taken into full account each side
Factor produces steady, efficient, low energy consumption the operation of High Purity Nitrogen, oxygen and liquid oxygen plant to realize.
Brief description of the drawings
Attached drawing in the present invention is only as the signal to the present invention, the spirit for understanding and explaining the present invention, but not in office
Where it is limited in face of the present invention.
Fig. 1 is the schematic diagram of one embodiment of the invention.
Embodiment
In the present invention, term " raw air " means the mainly mixture comprising oxygen and nitrogen.Term " theoretical tray " is anticipated
Refer to air-liquid two-phase on it to be all sufficiently mixed, and heat transfer and mass transport process resistance are 0 idealization column plate." distillation section "
Refer to there are certain intervals in destilling tower mutually, and each section all includes the structure of some rectifiying plates.
Referring to the drawings.First pass around a series of widely-known techniques dryings and purify raw air 101, the technology can
Including filter, temperature swing adsorbers etc..Such as raw air is removed the solid impurities such as dust by filter, then by molecule
Sieve clarifier or temperature swing adsorbers remove the foreign gas such as vapor and carbon dioxide.At least a portion of the subsequent raw air
The pressure close or equal with the operating pressure of the first destilling tower can be compressed to through main air compressor and is conveyed into the first main heat
Exchanger 1.
The low temperature logistics that first raw air 101 produces during being distillated in the first main heat exchanger 1 are cooled to one
As less than -150 DEG C and be transported to the first destilling tower 2 first distillation section 8, in the first destilling tower 2, cooled first
Raw air passes sequentially through the first distillation section 8, the 3rd distillation section 7, and is connect with main component for the phegma adverse current of liquid nitrogen
Touch.Therefore, the oxygen in gas phase and the boiling point component (methane, krypton, xenon etc.) higher than oxygen are dissolved in phegma, and in liquid phase
In nitrogen and the boiling point component (neon, hydrogen, helium etc.) lower than nitrogen be evaporated and be released into gas phase.As a result, in distillation section
Top formed the first nitrogen rich vapor 105 and 114, the first destilling tower 2 bottom of towe formation the first oxygen enriched liquid 103 and 135.The
A part of first oxygen enriched liquid 103 can be transported to the first condenser 3 of the first destilling tower 2 after throttle valve expands.
The first nitrogen rich vapor of Part I 105 at the top of distillation section is via Pipeline transport to the first condenser unit
In 4, by carrying out indirect heat exchange with being transported to the first oxygen enriched liquid of Part I 103 after the expansion of the first condenser 3
And be condensed, generation Part I richness nitrogen condensate liquid 111, Part I richness nitrogen condensate liquid can return to the distillation of the first destilling tower 2
Taken out as phegma or as liquid nitrogen product 112 via pipeline portions at the top of section.
In the first condenser 3, due to indirect heat exchange, the first oxygen enriched liquid 103 at least partly gasifies, in the first condensation
The hyperoxia quantity of fluid 113 of liquid phase and the steam phase of rich nitrogen, i.e. the second nitrogen rich vapor 125 are produced in the housing of device 3.Hyperoxia quantity of fluid
113 are transported to the second condenser 5 upon inflation.Second nitrogen rich vapor has higher oxygen content compared with raw air, its oxygen
Content is generally in 25~29 mole percents.
The first nitrogen rich vapor of Part II 114 at the top of distillation section is via Pipeline transport to the second condenser unit
6, by being condensed with being transported to the progress indirect heat exchange of hyperoxia quantity of fluid 113 of the second condenser 5, generate Part II
Rich nitrogen condensate liquid 115, Part II richness nitrogen condensate liquid can return to the top of the distillation section of the first destilling tower 2 as phegma or
Taken out as liquid nitrogen product 112 via pipeline portions.
Hyperoxia quantity of fluid in second condenser 5 at least partly gasifies by indirect heat exchange, generates the first waste stream 121,
Expanded respectively by the heating of the first main heat exchanger 1 and expanding machine 30, and in the first main heat exchanger 1 with raw air into one
Indirect heat exchange is walked, is further heated up and is discharged as waste gas stream.Oxygen content in first waste stream is generally higher than 46 Mole percents
Number.
The second nitrogen rich vapor of at least part 125 formed in the first condenser 3 is formed first through the first compressor 31
The first circulation stream 132 cooled down by the first main heat exchanger 1, is transported to the after-fractionating of the first destilling tower 2 by recycle stream 131
Section 9.Wherein, after-fractionating section 9 is positioned at 8 lower section of the first distillation section and at least one theoretical cam curve in interval.
In a preferred embodiment of the invention, 30 and first compressor 31 of expanding machine be it is mechanically connected connect, therefore
The part energy discharged during gas expansion can be used directly for compression.Simultaneously as liquid stream quilt in the first condenser 3
Discharge so that containing less oxygen in the logistics of evaporation, and the first condenser 3 can maintain higher pressure, so that the gas
In compressor compresses, required work lowers, and can have high flow again when the input work of isodose gives the first compressor 31
Recycle stream.The high flow capacity of recirculation flow makes the first destilling tower 2 have high nitrogen recovery with high nitrogen concentration.
Alternatively, at least partly the first nitrogen rich vapor 105 and 114 can be taken off as nitrogen product 151.
The second oxygen enriched liquid 160 is extracted in remaining hyperoxia quantity of fluid 113 after being vaporized from the second condenser 5, it is expanded
After-fractionating tower 40 is sent into afterwards, and the second oxygen enriched liquid 160 after expansion includes the gentle body portion of liquid portion, the liquid portion
The after-fractionating tower reboiler 44 positioned at 40 lower part of after-fractionating tower is flowed down to, the gas part rises and given birth at top
Into the second waste stream 164, after which flows through 33 re-heat of the second main heat exchanger, at least partly pressed through the second compressor 32
Second circulation stream 165 is generated after contracting, in the second main heat exchanger 33, second circulation stream 165 with it is compressed after purification second
Raw air 161, can input after-fractionating tower with after 174 and second waste stream of high pressure liquid oxygen, 164 indirect heat exchange and cooling
Lower space 43.
After-fractionating tower lower space 43 contains oxygen deprivation steam and poor oxygen liquid, and at least part oxygen deprivation steam 166 is as warm
Source is conveyed into after-fractionating tower reboiler 44, and the second oxygen enriched liquid indirect heat exchange after rectifying, and at least partly condenses
Generate poor oxygen liquid 167 and return to after-fractionating tower lower space 43.Extract remaining second liquid in after-fractionating tower reboiler 44
Oxygen 173, can export in the second main heat exchanger 33 after the supercharging of liquid oxygen pump 34 after re-heat as the second oxygen product 175.
Extract the poor oxygen liquid in after-fractionating tower lower space 43 and be divided at least two parts, the poor oxygen liquid of Part I
162 it is expanded after be introduced into after-fractionating tower upper space 41 and be used as phegma, can after the poor oxygen liquid 163 of Part II is expanded
Mixed with the first oxygen enriched liquid 103 with 135 and be admitted to the first condenser 3.
A part for phegma is extracted from the 3rd distillation section 7, it is defeated after the liquid air 133 as no high boiling component is expanded
It is sent to the top of the 3rd destilling tower 20.Wherein, the 3rd distillation section 7 is located at positioned at the first distillation section 8 top and interval at least
One theoretical cam curve.
The liquid air without high boiling component after expansion includes the gentle body portion of liquid portion, in the 3rd destilling tower upper space
The gas part of 21 portion collection gas-liquid mixtures, its liquid portion is as phegma down through the 3rd distillation column distillation
Section 22, liquid discharges low boiling component so as to improve the oxygen content of liquid in the section.In the 3rd destilling tower lower part
The 3rd destilling tower reboiler 24 that liquid is collected for heating lower space is installed, in the 3rd destilling tower reboiler in space 23
Liquid portion and 135 indirect heat exchange of the first oxygen enriched liquid of Part II introduced from the first destilling tower 2 in 24, than oxygen boiling point
Low component (argon, carbon dioxide, nitrogen etc.) is selectively evaporated, and rises through the 3rd destilling tower distillation section 22.Finally
The nitrogen of low boiling component containing than oxygen low boiling point is collected in the 3rd destilling tower upper space 21, distills tower bottom the 3rd
Ultra-high purity liquid oxygen, i.e. the 3rd liquid oxygen product 145 are generated, the first oxygen enriched liquid of Part II after cooling is transmitted back to the 1st
Or second condenser 5.
The 3rd waste stream 143 is collected in the 3rd destilling tower upper space 21 and (contains the low boiling point group than oxygen low boiling point
Point), through demi-inflation, alternatively, merge with the first expanded waste stream, in the first main heat exchanger 1 with the first raw material
Air indirect heat exchange, is further heated up as waste gas stream.
In the 3rd destilling tower reboiler 24, its heat source is oxygen-enriched for the Part II first that 2 bottom of towe of the first destilling tower is formed
Liquid 135, into the 3rd destilling tower reboiler 24, is cooled after carrying out indirect heat exchange with first oxygen enriched liquid 135,
The first oxygen enriched liquid of Part II 141 after cooling is transmitted back to the first or second condenser after demi-inflation.
Wherein, at least partly first waste stream and/or first raw air expand in expanding machine, are
The above process provides required cold.
Embodiment：
According to technique proposed by the present invention, the process units of a nitrogen is manufactured, the nitrogen oxygen content that it is produced is no more than
1ppm, the air pressure of product nitrogen output is 9.5bar, flow 10000Nm3/h；The process units of a high pure oxygen has also been manufactured,
The oxygen amount containing argon that it is produced is no more than 100ppb, and the pressure of high pure oxygen product output is 1.5bar, flow 129Nm3/h.At the same time
The process units of an oxygen is also manufactured, the air pressure of product oxygen output is 7.5bar, flow 315Nm3/ h, and contain volume integral
Number is 0.5% argon.
20 DEG C, 9.8bar, 19740Nm3The drying of/h and (the actually anhydrous and CO of pure air stream 1012) into first
Before first distillation section 8 of destilling tower 2, initially enter the first main heat exchanger 1 and be cooled to -164.3 DEG C.
Oxygen content is 38.2 mole percents, flow 15850Nm3The Part I oxygen enriched liquid 103 of/h is steamed from first
Evaporate the bottom discharge of tower 2, the first oxygen enriched liquid of Part I 103 of 35.6% volume fraction is transported to the after throttle valve expands
First condenser 3 of one destilling tower 2, the first oxygen enriched liquid of Part II 135 for being left 64.4% volume fraction are used as heat source quilt
Be transported to the 3rd destilling tower reboiler 24, be transmitted back to after the first oxygen enriched liquid 141 after cooling is expanded first condenser 3 or
Second condenser 5.
Oxygen content is 26.8 mole percents, flow 7980Nm3The second nitrogen rich vapor 125 of/h -171.2 DEG C,
6.0bar is exported by the first condenser 3, and the second nitrogen rich vapor 125 is first after the first compressor 31 is compressed to 9.8bar, then pass through
First main heat exchanger 1 cools down and is transported to the after-fractionating section 9 of the first destilling tower 2.
The hyperoxia quantity of fluid 113 for the surplus being sent into the first condenser 3 by being sent into after expansion in the second condenser 5,
4.7bar, -171.2 DEG C of gasifications.
Gaseous first waste stream 121 is sent into the first main heat exchanger 1 and is warming up to -140.7 DEG C, then in expanding machine
After 30 expansions, it can merge with the 3rd waste stream 143 of the top of the 3rd destilling tower 20 generation, reenter the first main heat exchanger 1,
18 DEG C are warming up to herein.The waste stream is with 9660Nm3The flow discharge of/h, oxygen content therein is 39.1 mole percents.
By -170.0 DEG C, 9.7bar, 10000Nm of the discharge of the top of the first destilling tower 23The first nitrogen rich vapor 151 of/h,
Transferred out after being warming up to 18 DEG C in first main heat exchanger 1 using 9.5bar and be used as High Purity Nitrogen product.
From the 3rd of the first destilling tower 2 distillation section 7 extract -168.3 DEG C of no high boiling component, 9.7bar,
1890Nm3/ h, the liquid air 133 without high boiling component that oxygen content is 11.6 mole percents, are conveyed into the 3rd after expansion
The upper space of destilling tower 20.
- 178.7 DEG C, 1.5bar, 129Nm are extracted in the bottom of the 3rd destilling tower 203High-purity oxygen liquid of/h is simultaneously used as the
Three liquid oxygen products 145 export.The 3rd waste stream 143 is generated in the upper space of the 3rd destilling tower 20, alternatively, with the first waste
Stream 121 merges.
- 171.2 DEG C, 4.7bar, 448Nm are extracted after being vaporized from the second condenser 5 in remaining hyperoxia quantity of fluid 1133/
H, oxygen content is the second oxygen-enriched liquid 160 of 70.0 mole percents, and after-fractionating tower 40 is sent into after expanded.
- 181.4 DEG C, 3.1bar, 1060Nm are generated at the top of after-fractionating tower 403/ h, oxygen content are 14.3 mole hundred
Second waste stream 164 of fraction, second waste stream 164 flow through the second main heat exchanger 33 and are warming up to 18 DEG C, 91.7% volume
Second waste stream of fraction is compressed to 9.7bar by the second compressor 32, after by the second main heat exchanger 33 be input to second
Destilling tower lower space 43；Second waste stream of remaining 8.3% volume fraction is discharged after purifying and expanding as exhaust gas.
20 DEG C, 20.9bar, 435Nm3The drying of/h and pure high pressure air flow 161, initially enter the second main heat exchanger
33 are cooled to -163.5 DEG C, after be input to after-fractionating tower lower space 43.
1410Nm is extracted in after-fractionating tower lower space 433/ h, the oxygen deprivation liquid that oxygen content is 16.4 mole percents
Body.41 conduct of after-fractionating tower upper space is introduced into after the poor oxygen liquid 162 of Part I of 65.9% volume fraction is expanded
Phegma, can be with the first oxygen-rich liquid of Part I after the poor oxygen liquid 163 of Part II of remaining 34.1% volume fraction is expanded
Body 103 mixes and is admitted to the first condenser 3.
Extract -170.6 DEG C, 3.1bar, 315Nm in after-fractionating tower reboiler 443The second liquid oxygen 173 of/h, can be through liquid
Oxygen pump 34 boosts to 7.7bar, defeated using 18 DEG C, 7.5bar as the second oxygen product after the heating of the second main heat exchanger 33
Go out.
Claims (5)
1. the method for High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification, including：
(a) compressed the first raw air (101) after purification is provided to the first distillation section (8) of the first destilling tower (2)；
(b) first raw air is separated into the first nitrogen rich vapor on top in first destilling tower (2)
(105,114) and bottom of towe the first oxygen enriched liquid (103,135)；
(c) the first nitrogen rich vapor of Part I (105) and the first oxygen enriched liquid of Part I (103) are between the first condenser (3)
Heat exchange is connect, makes the first nitrogen rich vapor of Part I (105) condensation generation Part I richness nitrogen condensate liquid (111), and make first
Oxygen enriched liquid (103) at least partly vaporizes, the second nitrogen rich vapor of generation (125) and hyperoxia quantity of fluid (113)；
(d) at least part of hyperoxia quantity of fluid (113) and the first nitrogen rich vapor of Part II (114) the second condenser (5) into
Row indirect heat exchange, makes the first nitrogen rich vapor of Part II (114) condensation generation Part II richness nitrogen condensate liquid (115), makes institute
State hyperoxia quantity of fluid (113) at least partly to vaporize, the first waste stream of generation (121)；
(e) first destilling tower (2) is returned to using the rich nitrogen condensate liquid (111,115) described at least part as phegma；
(f) the second nitrogen rich vapor (125) described at least part is formed into first circulation stream (131) through the first compressor (31),
The after-fractionating section of the first destilling tower (2) will be conveyed into by the first circulation stream (132) of the first main heat exchanger (1) cooling
(9), wherein, after-fractionating section (9) is positioned at the first at least one theoretical cam curve in distillation section (8) lower section and interval；
(g) the second oxygen enriched liquid (160), warp are extracted after vaporization in remaining hyperoxia quantity of fluid (113) from the second condenser (5)
After-fractionating tower (40) is sent into after expansion, the second oxygen enriched liquid (160) after expansion includes the gentle body portion of liquid portion, described
Liquid portion flows down to the after-fractionating tower reboiler (44) positioned at after-fractionating tower (40) lower part, on the gas part
Rise and generate the second waste stream (164) at top, after which flows through the second main heat exchanger (33) re-heat, at least partly
Second circulation stream (165), in the second main heat exchanger (33), second circulation stream are generated after the second compressor (32) compression
(165) with compressed the second raw air (161) after purification, can with high pressure liquid oxygen (174) and the second waste stream (164)
After indirect heat exchange and cooling, after-fractionating tower lower space (43) is inputted；
(h) after-fractionating tower lower space (43) contains oxygen deprivation steam and poor oxygen liquid, at least part oxygen deprivation steam (166) conduct
Heat source is conveyed into after-fractionating tower reboiler (44), and the second oxygen enriched liquid indirect heat exchange after rectifying, and at least partly
Condensation generates poor oxygen liquid (167) and returns to after-fractionating tower lower space (43)；Extract in after-fractionating tower reboiler (44) and remain
Remaining the second liquid oxygen (173), can be used as the second oxygen after liquid oxygen pump (34) supercharging in the second main heat exchanger (33) after re-heat
Gas product (175) exports；
(i) extract the poor oxygen liquid in after-fractionating tower lower space (43) and be divided at least two parts, Part I oxygen deprivation liquid
After-fractionating tower upper space (41) is introduced into after body (162) is expanded and is used as phegma, the poor oxygen liquid of Part II (163) warp
It can be mixed after expansion with the first oxygen enriched liquid (103,135) and be admitted to the first condenser (3)；
(j) part for phegma is extracted from the 3rd distillation section (7) of the first destilling tower (2), as no high boiling component
The top of the 3rd destilling tower (20) is conveyed into after liquid air (133) is expanded, wherein, the 3rd distillation section (7) is positioned at the first distillation
At least one theoretical cam curve in above section (8) and interval；
(k) liquid air without high boiling component after expanding includes the gentle body portion of liquid portion, and the liquid portion flows downward
To the 3rd destilling tower reboiler (24) positioned at the 3rd destilling tower (20) lower space, with introduced from the first destilling tower (2)
Two part the first oxygen enriched liquid (135) indirect heat exchanges, and generate the 3rd liquid oxygen product in the bottom of the 3rd destilling tower (20)
(145), the first oxygen enriched liquid of Part II (141) after cooling is transmitted back to first (3) or the second condenser (5)；
(l) the 3rd waste stream (143) is generated in the 3rd destilling tower upper space (21), alternatively, is closed with the first waste stream (121)
After and, in the first main heat exchanger (1) and compressed the first raw air (101) indirect heat exchange after purification；
(m) alternatively, at least partly the first nitrogen rich vapor (105,114) can be taken off as nitrogen product (151)；
(n) alternatively, at least partly rich nitrogen condensate liquid (111,115) can be taken off as liquid nitrogen product (112)；
Wherein, at least partly described first waste stream (121) and/or first raw air (101) are in expanding machine (30)
Expand, required cold is provided for the cryogenic rectification process.
2. the method for claim 1, wherein first compressor (31) and expanding machine (30) are mechanical communications
's.
3. a kind of equipment for producing High Purity Nitrogen, oxygen and liquid oxygen from air by cryogenic rectification, including：
(a) equipment that compress raw air, purifies and the logistics for generating itself and cryogenic rectification carry out indirect heat exchange with the
Connected the first main heat exchanger (1) of one destilling tower (2) and the second main heat exchanger (33) being connected with after-fractionating tower (40)；
(b) the first destilling tower (2), comprising some distillation sections, compressed, purifying, cooling are provided to the first distillation section (8)
First raw air (101), is separated into first nitrogen rich vapor (105,114) on top and the first oxygen enriched liquid of bottom of towe
(103,135)；
(c) the first condenser (3), wherein, the first oxygen enriched liquid of the first nitrogen rich vapor of Part I (105) and Part I
(103) in the first condenser (3) indirect heat exchange, make the first nitrogen rich vapor of Part I (105) condensation generation Part I rich
Nitrogen condensate liquid (111), makes first oxygen enriched liquid of Part I (103) at least partly vaporize, and generates the second nitrogen rich vapor
(125) and hyperoxia quantity of fluid (113)；
(d) the second condenser (5), wherein, at least part of hyperoxia quantity of fluid (113) and the first nitrogen rich vapor of Part II
(114) indirect heat exchange is carried out in the second condenser (5), makes the first nitrogen rich vapor of Part II (114) condensation generation second
Separation nitrogen-enriching condensate liquid (115), makes the hyperoxia quantity of fluid (113) at least partly vaporize, the first waste stream of generation (121)；
(e) equipment of the first destilling tower (2) as phegma will be sent back to incite somebody to action at least partly rich nitrogen condensate liquid (111,115)；
(f) the second nitrogen rich vapor (125) to be compressed through the first compressor (31), as first circulation stream (131) cooling simultaneously
Send to the equipment of the after-fractionating section (9) of the first destilling tower (2), wherein, after-fractionating section (9) is positioned at the first distillation section
(8) at least one theoretical cam curve in lower section and interval；
(g) using remaining hyperoxia quantity of fluid (113) after vaporization in the second condenser (5) as the second oxygen enriched liquid (160) through swollen
The pipeline and expansion valve of after-fractionating tower (40) are sent into after swollen；
(h) after-fractionating tower (40), after-fractionating tower upper space (41), after-fractionating tower distillation section (42), after-fractionating
Tower lower space (43) and the after-fractionating tower reboiler (44) for reboiling liquid oxygen；
(i) the second main heat exchanger (33) re-heat is inputted from after-fractionating tower upper space (41) by the second waste stream (164), and
Defeated time the second main heat exchanger (33) cooling, then input after-fractionating tower lower space again after the second compressor (32) compression
(43) pipeline；
(j) pressurized, purifying the second raw air (161) is inputted into the second main heat exchanger (33) cooling, then inputs second
The pipeline of destilling tower lower space (43)；
(k) the oxygen deprivation steam (166) in after-fractionating tower lower space (43) is conveyed into after-fractionating tower reboiler (44)
Pipeline, and condensed poor oxygen liquid (167) is transmitted back to the pipeline of after-fractionating tower lower space (43)；
(l) conveyed after the second liquid oxygen (173) in after-fractionating tower reboiler (44) is pressurized alternatively through liquid oxygen pump (34)
Enter the second main heat exchanger (33) re-heat, and as the pipeline of the second oxygen product output；
(m) the poor oxygen liquid in after-fractionating tower lower space (43) is conveyed into after-fractionating tower upper space (41) respectively
Pipeline (162) and the pipeline (163) converged with the first oxygen enriched liquid；
(n) be located in the first destilling tower (2), above the first distillation section (8) and at least one theoretical cam curve in interval the
Three distillation sections (7), a part for phegma, the liquid air as no high boiling component are extracted from the described 3rd distillation section (7)
(133) equipment at the top of the 3rd destilling tower (20) is conveyed into after expanded；
(o) be located at the 3rd destilling tower (20) lower space the 3rd destilling tower reboiler (24), wherein, after expansion without higher boiling
Liquid portion in the liquid air of component, flows through the distillation section (22) of the 3rd destilling tower (20), herein with drawing from the first destilling tower
The first oxygen enriched liquid of Part II (135) indirect heat exchange entered, and generate the 3rd liquid oxygen in the bottom of the 3rd destilling tower (20)
Product (145), the first oxygen enriched liquid of Part II (141) after cooling are transmitted back to first (3) or the second condenser (5)；
(p) the 3rd waste stream (143) that will be generated at the top of the 3rd destilling tower (20), alternatively, with the first waste stream (121)
After merging, the equipment to the first main heat exchanger (1) and the first raw air (101) indirect heat exchange is sent；
(q) expanding machine (30), at least partly first waste stream (121) and/or first raw air will expand and be
Cryogenic rectification process provides required cold.
4. equipment as claimed in claim 3, wherein, first compressor (31) and expanding machine (30) they are mechanical communications
's.
5. the equipment as described in claim 3 or 4, wherein, the first condenser (3), the second condenser (5) and reboiler (24,
44) it is made of plate heat exchanger.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711464387.6A CN108036584A (en) | 2017-12-28 | 2017-12-28 | The method and apparatus of High Purity Nitrogen, oxygen and liquid oxygen is produced from air by cryogenic rectification |
Applications Claiming Priority (1)
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| CN112524886A (en) * | 2019-09-18 | 2021-03-19 | 乔治洛德方法研究和开发液化空气有限公司 | High purity oxygen production system |
| WO2021078405A1 (en) | 2019-10-23 | 2021-04-29 | Linde Gmbh | Method and system for low-temperature air separation |
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