CN103988037A - Air separation method and apparatus - Google Patents

Air separation method and apparatus Download PDF

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Publication number
CN103988037A
CN103988037A CN201280059867.3A CN201280059867A CN103988037A CN 103988037 A CN103988037 A CN 103988037A CN 201280059867 A CN201280059867 A CN 201280059867A CN 103988037 A CN103988037 A CN 103988037A
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China
Prior art keywords
stream
oxygen
liquid
destilling tower
nitrogen
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Granted
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CN201280059867.3A
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Chinese (zh)
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CN103988037B (en
Inventor
H.E.霍瓦尔德
M.R.怀特
T.J.伯格曼
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Praxair Technology Inc
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Praxair Technology Inc
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Priority claimed from US13/311,038 external-priority patent/US20130139546A1/en
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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
    • 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
    • F25J3/04103—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 using solely hydrostatic liquid head
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F25J3/04212—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product and simultaneously condensing vapor from a column serving as reflux within the or another column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • F25J3/0423—Subcooling of liquid process streams
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04254—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using the cold stored in external cryogenic fluids
    • 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
    • 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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
    • 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
    • F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
    • F25J3/04884—Arrangement of reboiler-condensers
    • 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
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • 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
    • 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
    • F25J2210/42—Nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/50—Oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/44—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop

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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

A method and apparatus to produce oxygen and nitrogen co-products in which a compressed a compressed and purified air stream is cooled, fully or partially condensed and then rectified in a main distillation column to form a nitrogen-rich vapor column overhead and crude liquid oxygen. A crude liquid oxygen stream is depressurized and then stripped in an auxiliary distillation column with a stripping gas to produce an oxygen-rich liquid. The nitrogen-rich vapor column overhead from the main distillation column is used to form a nitrogen product and the crude liquid oxygen is partially vaporized to produce the stripping gas, a residual oxygen-rich liquid and liquid nitrogen reflux to the main distillation column. The oxygen product is formed from the residual oxygen-rich liquid by either providing the heat exchange duty in condensing the compressed and purified air stream or by condensing nitrogen-rich vapor used in refluxing the main distillation column.

Description

Air separating method and device
 
Invention field
The present invention relates to a kind of method and apparatus for separating of air, wherein by compressed and air purifying being carried out to rectifying in main destilling tower, produce nitrogen product, and by formed thick liquid oxygen in main destilling tower being carried out to stripping in auxiliary destilling tower, produce oxygen product, produce thus oxygen product and nitrogen product as joint product (co-products).
background of invention
Conventionally, by the low temp air fractionation system often adopting simple distillation tower from air separating off nitrogen, and obtain nitrogen with high-purity.In this equipment, then air compressing is removed to higher impurity to produce compressed and air stream purifying.Then in main heat exchanger inside, compressed and air stream purifying is cooled to be suitable for the temperature of its cryogenic rectification, is then imported at approximately 3 bar or the single distillation column that more operates under high pressure.Air in destilling tower inside is carried out to rectifying, to produce nitrogen rich vapor overhead and the oxygen enriched liquid bottoms that is called as thick liquid oxygen or still liquid.In expansion valve by oxygen enriched liquid decompression, then by its delivery heat exchanger so that the condensation of nitrogen rich vapor overhead stream is created in the liquid nitrogen refluxing in destilling tower thus.The oxygen enriched liquid partly being evaporated can be used to form the refrigeration for equipment, or alternatively by liquid nitrogen being added to king-tower or making to flow to into main heat exchanger, can provide refrigeration to equipment.
Conventionally, from this single tower nitrogen equipment, do not reclaim oxygen.Yet, also there is the interest that reclaims oxygen from this equipment.For example, conventionally to need flow-rate ratio be nitrogen and the low purity oxygen of about 2:1 to float glass.In glass furnace, utilize oxygen to improve the rate of recovery and conventionally need to be at the oxygen of the low-purity between 90 and 95% and the pressure between 10 and 20 psig.Although can utilize independent Vacuum pressure swing adsorption equipment or provide this oxygen by the on-the-spot liquid evaporation that makes to carry, the expense increasing is irrational.It should be pointed out that and can utilize the double-tower air separation equipment typically with high-pressure tower and lower pressure column to produce oxygen and nitrogen in operationally relevant to heat transfer relation mode.Yet for example, due to the requirement of product compression and higher initial stage fund cost (producing float glass), thereby this equipment is uneconomic.To meeting economically the requirement of technique for exporting the modification of increase of little single tower nitrogen equipment of nitrogen and oxygen product, for example float glass, wherein need to (being for example less than the nitrogen of 100 standard cubic foots/hour (kcfh)) provide nitrogen and oxygen product under pressure and under appropriate flow.
In the prior art, exist and to be modified and the example of single tower nitrogen equipment of coproduction nitrogen and oxygen product.For example, at US 4,783, in 210, in the heat exchanger of the stream condensation of the nitrogen rich vapor overhead for making to produce at destilling tower, thick liquid oxygen tower base stream is partly evaporated.Formed nitrogen-rich liquid is for refluxing at destilling tower.Then, the stream of the gained liquid phase producing by thick liquid oxygen partial gasification is carried out in secondary or auxiliary destilling tower to stripping to produce rich oxygen containing bottoms, at the bottom of this tower, can not be taken as oxygen product.By another nitrogen enriched vapor stream, auxiliary destilling tower is seethed with excitement again, the condensation and can be taken as liquid nitrogen product and also for refluxing at destilling tower in boiling again of this nitrogen enriched vapor stream.
US 5,074, disclose a kind of single tower nitrogen-making device in 898, and auxiliary destilling tower is produced oxygen product.In this patent, in auxiliary destilling tower, the thick liquid oxygen stream producing is carried out to stripping in main destilling tower.The stream of the nitrogen rich vapor overhead that utilization produces in main destilling tower seethes with excitement auxiliary destilling tower again.Thereby make thus nitrogen rich vapor condensation be formed on the backflow in main destilling tower.The remaining liq producing in auxiliary destilling tower can be taken as fluid product together with part through condensation nitrogen steam.
In above-mentioned two patents, bottoms is used for making nitrogen condensation, must under the pressure lower than nitrogen, complete nitrogen condensation.As a result, oxygen product is also in low-pressure state.In addition, because the bottoms of part is taken as product, so less for making liquid at the bottom of the tower of nitrogen condensation by existing.Therefore, nitrogen output is restricted.As what will discuss hereinafter, the invention provides a kind of method and apparatus for the production of nitrogen and oxygen joint product, except other advantage, the method and device allow to produce oxygen product under the pressure raising.In another aspect of this invention, thus stand-by still substrate can obtain larger oxygen mark with energy consumption lower than institute's adopting process in prior art through stage evaporation.
Summary of the invention
The invention provides a kind of by air separation to produce the method for oxygen and nitrogen co-product.According to this method, in main destilling tower inside, compressed and the aeriferous stream of bag purifying are carried out to cooling and rectifying, to produce nitrogen rich vapor overhead and thick liquid oxygen.By at least in part the thick liquid oxygen stream being comprised of thick liquid oxygen being reduced pressure, at the inner stripping gas with rising of auxiliary destilling tower, thick liquid oxygen stream is carried out to stripping, and by the nitrogen enriched vapor stream with being formed by nitrogen rich vapor overhead, carry out indirect heat exchange oxygen enriched liquid is partly evaporated, and at the inner auxiliary overhead that produces oxygen enriched liquid and contain the oxygen that is not less than 5.0 volume % of auxiliary destilling tower.As a result, produce thus liquid nitrogen stream, stripping gas and remaining oxygen enriched liquid.With at least part of liquid nitrogen stream, in main destilling tower, reflux.Represent to be for further processing to produce oxygen enriched liquid and auxiliary overhead in auxiliary destilling tower inside with the phrase " at least in part " of claim use herein.As described hereinafter, although stand-by still can be only for thick liquid oxygen stream is carried out to stripping, it also can reclaim to improve oxygen for the steam of the nitrogenous and oxygen being produced by above-mentioned stripping being carried out to rectifying.
By remaining oxygen enriched liquid stream with have the nitrogen concentration that is not less than air nitrogen concentration gaseous flow indirectly exchanged heat make remaining oxygen enriched liquid stream by partial gasification, and form oxygen-rich steam cut by remaining oxygen enriched liquid.By vapor fraction, form oxygen product and flow, by nitrogen rich vapor, form nitrogen product stream, by assisting the auxiliary overhead of destilling tower to form waste stream.Make the stream of oxygen product stream, nitrogen product stream and waste stream and compressed and purifying carry out indirect heat exchange.
As understandable from discuss above, the vapor fraction correspondingly being produced by remaining oxygen enriched liquid because serving as reasons forms oxygen product and flows, so the production of oxygen product is no longer contacted directly with the production of backflow nitrogen for main destilling tower, because remaining oxygen enriched liquid is not used to make the nitrogen rich vapor condensation of autonomous destilling tower.As a result, the removal of remaining oxygen enriched liquid does not reduce to the nitrogen backflow of main destilling tower and does not therefore reduce nitrogen output, as situation of the prior art.
In addition, because remaining oxygen enriched liquid is not used to make nitrogen condensation, so can produce this liquid under elevated pressures.
As mentioned above, can only by thick liquid oxygen stream being carried out to stripping in auxiliary destilling tower inside, produce auxiliary overhead.Alternatively, with the liquid nitrogen stream of part, in main destilling tower, reflux.In the latter case, in auxiliary distillation exhausting section of column inside, thick liquid oxygen stream is carried out to stripping and stripping produces the steam flow that contains nitrogen and oxygen.By the steam flow that contains nitrogen and oxygen being imported to rectifying section and refluxing and therefore reflux in rectifying section with another part liquid nitrogen stream, and in the auxiliary destilling tower inside that is arranged in the rectifying section of the auxiliary destilling tower above stripping section, the steam flow that contains nitrogen and oxygen is carried out to rectifying in auxiliary destilling tower.This effect is by effectively fettering otherwise the oxygen that the oxygen of the waste stream inside of the stand-by still of will escaping improves in remaining oxygen enriched liquid inside reclaims.
In above-mentioned any situation, oxygen enriched liquid can be collected in to the inside of auxiliary destilling tower.By making oxygen enriched liquid stream and nitrogen enriched vapor stream by once-through heat exchanger, oxygen enriched liquid partly be evaporated so that the remaining oxygen enriched liquid that forms stripping gas and collect as the bottoms of assisting destilling tower.
Gaseous flow can be compressed and stream purifying.Compressed and stream purifying is collected in separation container by partial condensation and by remaining oxygen enriched liquid stream in condenser.Liquid phase stream by forming in the inner liquid phase producing of separation container is imported to condenser and by carrying out indirect heat exchange and make liquid phase stream partly evaporate with compressed and stream purifying, produce two phase flow thus by liquid phase stream in condenser.This two phase flow is imported to separation container and in separation container inside, make liquid phase and the vapor phase separation of two phase flow, to form oxygen-rich steam cut and liquid phase together with the stream that is collected in the residue oxygen enriched liquid in separation container.Then, by discharge the stream of oxygen-rich steam cut from separation container, and form oxygen product stream.
In above-mentioned embodiment of the present invention, condenser can be arranged in main destilling tower bottom zone the air of condensation is mixed mutually with the liquid of the decline producing by rectifying, produces thus the thick liquid oxygen as bottoms in main destilling tower.In addition, can in main destilling tower, reflux with the liquid nitrogen stream of part, and waste stream and thick liquid oxygen stream indirectly exchanged heat in case before reducing pressure by thick liquid oxygen stream sub-cooled.
As formed substituting of gaseous flow by compressed and stream purifying, gaseous flow can be comprised of nitrogen rich vapor overhead.In this embodiment, by will be rich in liquid oxygen stream decompression and in the inside of thermosyphon reboiler, make remaining oxygen enriched liquid stream carry out indirect heat exchange with gaseous flow, and between remaining oxygen enriched liquid stream and gaseous flow exchanged heat indirectly.Part evaporation by residue oxygen enriched liquid stream produces vapor fraction and the condensation by gas flow produces condensate stream thus.This condensate stream is imported to main destilling tower as the backflow together with liquid nitrogen stream.
In the above-described embodiment, before thick liquid oxygen stream is reduced pressure, waste stream can be with thick liquid oxygen stream generation indirect heat exchange so that by thick liquid oxygen stream sub-cooled.
In any embodiment of the present invention, can be by the pressurization of remaining oxygen enriched liquid stream so that also by the pressurization of oxygen product stream.In addition, liquid nitrogen refrigerating conductance is become owner of to destilling tower to freeze.
The present invention also provide a kind of for separating of air to produce the device of oxygen and nitrogen joint product.This device comprises main heat exchanger, main destilling tower and auxiliary destilling tower.Main heat exchanger is configured to the compressed and aeriferous stream of bag purifying in addition cooling; Main destilling tower is configured to compressed and stream purifying to carry out rectifying to produce nitrogen rich vapor overhead and thick liquid oxygen.Auxiliary destilling tower is connected to main destilling tower, and be configured to, at the inner stripping gas with rising of auxiliary destilling tower, the thick liquid oxygen stream being comprised of thick liquid oxygen is carried out to stripping, and at least in part due to the auxiliary overhead that the stripping of thick liquid oxygen stream is produced to oxygen enriched liquid and contain the oxygen that is not less than 5.0 volume %.Expansion valve is between main destilling tower and auxiliary destilling tower, to thick liquid oxygen stream is reduced pressure before importing auxiliary destilling tower.
Be provided for by with by nitrogen rich vapor nitrogen enriched vapor stream that overhead forms, carry out indirect heat exchange oxygen enriched liquid partly evaporated, produce thus the device of liquid nitrogen stream, stripping gas and remaining oxygen enriched liquid.Oxygen enriched liquid part vaporising device is connected to main destilling tower, to reflux in main destilling tower with at least part of liquid nitrogen stream.Main heat exchanger is connected to main destilling tower and auxiliary destilling tower so that the nitrogen product stream being formed by nitrogen rich vapor and by the air stream of the formed waste stream of auxiliary overhead of auxiliary destilling tower and compressed and purifying exchanged heat indirectly.Also be provided for remaining oxygen enriched liquid stream with there is between the gaseous flow of nitrogen concentration of the nitrogen concentration that is not less than air indirectly exchanged heat so that the device that remaining oxygen enriched liquid stream part is evaporated.In addition, be provided for by remaining oxygen enriched liquid stream, being formed the device of oxygen-rich steam cut after part evaporation.Main heat exchanger is connected to oxygen-rich steam cut and forms device, main destilling tower and auxiliary destilling tower, so that the nitrogen product stream that is flowed, is comprised of nitrogen rich vapor overhead by the oxygen product of oxygen-rich steam fractional composition in main heat exchanger inside and the waste stream being comprised of the auxiliary overhead of assisting destilling tower and the stream generation indirect heat exchange of compressed and purifying.
Stand-by still can only possess thick liquid oxygen stream is carried out to steam stripped stripping section.Substitute as one, stand-by still can possess stripping section and be positioned at the rectifying section of stripping section top.In the latter case, in auxiliary distillation exhausting section of column, carry out the stripping of thick liquid oxygen stream and produce in stripping section entering for nitrogenous and steam flow oxygen being carried out to the steam flow of nitrogenous and oxygen of the rectifying section of rectifying.This rectifying is provided, and the oxygen being increased in thus in residue oxygen enriched liquid reclaims.Oxygen enriched liquid part vaporising device is connected to main destilling tower, to reflux in main destilling tower with the liquid nitrogen stream of part, oxygen enriched liquid part vaporising device is also connected to auxiliary destilling tower to therefore auxiliary destilling tower is refluxed in rectifying section with the liquid nitrogen stream of another part.Another expansion valve is between oxygen enriched liquid part vaporising device and auxiliary destilling tower, so that by the pressure of the extremely auxiliary destilling tower of the pressure decreased of the liquid nitrogen stream of another part.
In any embodiment of the present invention, auxiliary destilling tower can possess for collecting the device of oxygen enriched liquid.Oxygen enriched liquid part vaporising device is once-through heat exchanger, this heat exchanger be connected to auxiliary destilling tower and oxygen enriched liquid gathering-device in case by the oxygen enriched liquid stream that makes to be formed by oxygen enriched liquid by and in once-through heat exchanger inside, oxygen enriched liquid is partly evaporated, and residue oxygen enriched liquid collects as auxiliary destilling tower bottoms.Main destilling tower is connected to once-through heat exchanger, so as in once-through heat exchanger inside by nitrogen enriched vapor stream condensation.
Gaseous flow can be compressed and air stream purifying.In this case, remaining oxygen enriched liquid stream heat-exchange device and oxygen-rich steam cut formation device are condenser and separation container.Condenser is connected to main heat exchanger so that by compressed and stream partial condensation purifying.Separation container is connected to auxiliary destilling tower so that remaining oxygen enriched liquid stream collects in separation container.Separation container is connected to condenser, to will partly evaporate to produce the two phase flow being imported in separation container by the liquid phase stream forming in the inner liquid phase that produces of separation container in condenser.In separation container inside, make the liquid phase of two phase flow and vapor phase separation to form oxygen-rich steam cut and liquid phase, main heat exchanger is connected to separation container and flows to form oxygen product by oxygen-rich steam cut.
In the embodiment of the invention described above, condenser can be arranged in the bottom zone of main destilling tower so that the air of condensation mixes with the liquid by compressed and stream purifying are carried out to decline that rectifying produces, and usings and produces the thick liquid oxygen as the bottoms in main destilling tower.In addition, once-through heat exchanger can be connected to main destilling tower, to reflux in main destilling tower with the liquid nitrogen stream of part.Sub-cooled heat exchanger is connected to once-through heat exchanger, auxiliary destilling tower and expansion valve so that in the internal waste stream of sub-cooled heat exchanger and thick liquid oxygen stream exchanged heat indirectly, and by before expansion valve by thick liquid oxygen stream sub-cooled.
Substitute as one, gaseous flow can be comprised of nitrogen rich vapor.In this case, residue oxygen enriched liquid stream heat-exchange device and oxygen-rich steam cut formation device are consisted of the thermosyphon reboiler with housing.Housing is connected to stand-by still to receive remaining oxygen enriched liquid stream, another expansion valve between housing and stand-by still so that by the decompression of remaining oxygen enriched liquid stream.Thermosyphon reboiler is connected to main destilling tower to receive gaseous flow, thus by carrying out indirect heat exchange and by gaseous flow condensation, form oxygen-rich steam cut and condensate stream is discharged into main destilling tower as the backflow together with liquid nitrogen stream in enclosure interior thus with residue oxygen enriched liquid stream.Main heat exchanger is connected to housing, main destilling tower and auxiliary destilling tower, so that the oxygen product being formed by vapor fraction flows, the nitrogen product stream being formed by nitrogen rich vapor overhead, the waste stream being formed by the auxiliary overhead producing in the middle of auxiliary destilling tower is all in the inside of main heat exchanger and compressed and stream generation indirect heat exchange purifying.
In the above-described embodiment, sub-cooled heat exchanger is between auxiliary destilling tower, main destilling tower and main heat exchanger, so that waste stream and thick liquid oxygen stream generation indirect heat exchange before the waste stream before the decompression of thick liquid oxygen stream and in heating main heat exchanger.
In arbitrary embodiment of the present invention, main destilling tower can possess for importing liquid nitrogen refrigerating stream so that the top inlet of freezing.
accompanying drawing summary
Although the present invention be take, point out that clearly applicant thinks that the claim of its subject matter of an invention is end, it is generally acknowledged when by reference to the accompanying drawings and will understand better the present invention, wherein:
Fig. 1 is for implementing according to the schematic diagram of the air separation equipment of the inventive method.
Fig. 2 is for implementing according to the schematic diagram of the air separation equipment of the inventive method alternate embodiments.
Fig. 3 is for implementing according to the schematic diagram of another alternate embodiments of the air separation equipment of the inventive method.
describe in detail
With reference to Fig. 1, showing can coproduction oxygen and nitrogen product (" N 2" and " O 2") air separation equipment 1.
In the saturated or approximate temperature that compressed and air stream 10 purifying is cooled to be suitable for its rectifying saturated in the situation that in main heat exchanger 12.As understandable, air separation equipment 1 can be a part that needs compressed-air actuated device, and the part air that therefore can produce in this device forms compressed and air stream 10 purifying.Alternatively, can be by air compressing being arrived to the pressure between 70 psia to 90 psia conventionally, then to will for example, carrying out purifying and form this stream at the air of the curing or concentrated higher impurity (carbon dioxide, steam and hydro carbons) of cryogenic temperature.Main heat exchanger 12 can have conventional brazed aluminum plate fin structure.Just as the skilled person will appreciate, main heat exchanger 12 can be comprised of a plurality of unit of parallel work-flow.
After being cooled, the air stream of compressed and purifying 10 is imported to the condenser 14 of the base area 16 that is arranged in main destilling tower 18.Destilling tower 18 contains mass transfer contact element, for example combination of column plate, structured packing, random packing or this element, and these elements represent with reference number 20 conventionally.Preferably, in condenser 14 inside, by the air entering, partly condensation is to produce vapor fraction 22, and these vapor fraction 22 risings enter mass transfer contact element 20 and contact with the liquid phase that produces the decline of nitrogen rich vapor overhead 23.Nitrogen rich vapor overhead 23 is normally essentially pure nitrogen.The partial condensation of air produces liquid distillate 24, and this liquid distillate forms about 20% the liquid that enters air and decline together with 20 inside of the contact element in the base area 16 of main destilling tower 18 as thick liquid oxygen 26 and collects.
The replacement device that it should be pointed out that the air setting for making to enter will make condenser 14 be positioned at the outside of main destilling tower 18.Together with this device, can be individually by liquid distillate 24 with mixed to form thick liquid oxygen 26 or can and join individually in tower 34 their sub-cooled at the inner liquid declining of destilling tower 20.In another this device, compressed and air stream purifying directly can be imported to main destilling tower housing.Air will be allowed to mix with the steam of tower inside with from the recirculation steam 22 of condenser 14.In this structure, condenser will not have condensation side house steward, only by condensation, makes gas inflow heat exchanger.As another, substitute, can by a part through cooling-air stream 10, guide to the housing of tower 18, and utilize pipeline that portion of air stream 10 is directly delivered to condenser 14.This structure will allow product oxygen flow and nitrogen stream to regulate.Yet this structure will need extra valve and control device.Another device will adopt the independent air stream that can be further compressed.If this independent air stream is further compressed, will be separated at fire end, if or not compressed, separated at cold junction.Then, will be in condenser 14 inside by this air stream total condensation.Then through suitable pipeline, the air through condensation is imported to the intersegmental position of main destilling tower 18.Air through condensation will not be collected in the storage tank of this tower, but liquefied air is upwards joined several sections from the bottom of main destilling tower 14.
Then, preferably in the inside of sub-cooled heat exchanger 30, the thick liquid oxygen stream 28 being comprised of thick liquid oxygen 26 is carried out to sub-cooled, in the expansion valve 32 between main destilling tower 18 and stand-by still 34, thick liquid oxygen stream 28 is decompressed to the preferably pressure of 15 to 25 psia.Then, by making this stream contact in mass transfer contact element 36 and in auxiliary destilling tower 34 inside, thick liquid oxygen stream 28 be carried out to stripping with the stripping air-flow 52 of rising; Mass transfer contact element 36 can be the combination of column plate, structured packing, random packing or this element.Stripping produces auxiliary overhead 38, and this distillate 38 conventionally contains the nitrogen between 80 volume % to 90 volume % and conventionally contains the residue oxygen enriched liquid 56 of the oxygen of 85 volume % to 98 volume %.
Oxygen enriched liquid 40 can be collected in and collect the inside of column plate 42 or similarly in device, wherein collect the liquid that declines by and allow the steam that rises by and enter mass transfer contact element 36.By the nitrogen rich vapor 23 with by once-through heat exchanger 48 inside form nitrogen enriched vapor stream 46 and carry out indirect heat exchange, and the stream of the oxygen enriched liquid 44 that is comprised of oxygen enriched liquid 40 is partly evaporated.As the result of indirect heat exchange, produce liquid nitrogen stream 50.Make oxygen enriched liquid flow 44 parts and evaporate to produce stripping gas 52 and remaining gas liquid stream 54, the bottom that remaining gas liquid stream 54 collects in auxiliary destilling tower 34 is as remaining oxygen enriched liquid 56.It should be noted that, in alternate embodiments, can from auxiliary destilling tower 34, extract the two phase flow from the boiling lateral of once-through heat exchanger, and this two phase flow is guided to an independent phase separator to produce remaining stream of oxygen-enriched liquid 68, then utilize pipeline that vapor phase is delivered to auxiliary destilling tower 34 to form stripping gas 52.Although be not preferred, this embodiment will be equal to the embodiment shown in accompanying drawing.
As the replacement device of once-through heat exchanger 48 and collection column plate 42, can utilize the thermosyphon reboiler that is positioned at stand-by still 34 base portions to make oxygen enriched liquid 40 parts evaporations from mass transfer contact element 36, drop to the base portion of stand-by still 34.The core of this reboiler will be positioned at the inside of residue oxygen enriched liquid, and by making oxygen enriched liquid 40 evaporations produce stripping gas.Yet this will not be preferred, considers that this heat exchanger will can not utilize the temperature difference of once-through heat exchanger to operate; Subsequently must be by the air compressing entering to elevated pressures.
As shown in the figure, liquid nitrogen stream 50 (its whole or its part) can be imported to main destilling tower 18 as reflow stream 58.By remainder that auxiliary overhead 38 forms, as other liquid nitrogen stream 60 (being depressurized by valve 63) and waste stream 62, thereby can first be imported into sub-cooled heat exchanger 30, carry out indirect heat exchange by its sub-cooled with thick liquid oxygen stream 28, thereby then carry out indirect heat exchange with the air stream 10 of the compressed and purifying entering, contribute in main heat exchanger 12 inside it is cooling.Alternatively, stream 60 can be mixed and heats with stream 62.After being heated, will from main heat exchanger 12, discharge as gaseous nitrogen joint product (" N 2") other liquid nitrogen stream 60, and can be by waste stream 62 for making for the air entering being carried out to the regeneration of the adsorbent that the pre-purification unit of prepurification adopts and for air separation equipment 1.In addition, also can be by mixing with the air entering by its recompression and by it, and make all or part of this stream recirculation.The application that it should be pointed out that stream 60 is optional, and the object of the evaporation of liquid nitrogen stream 60 is extra sub-cooled is provided and therefore can realizes larger oxygen yield to stream 28.
It should be pointed out that and can before by valve 63, from the intersegmental position of tower 20, extract liquid nitrogen reflux stream 60.
Also be to be noted that and the sub-cooled heat exchanger 30 being discussed or 30' and main heat exchanger 12 can be combined.Equally likely, do not adopting this sub-cooled heat exchanger 30 or 30 ' in the situation that form an embodiment of the invention.Under any circumstance, in this illustrated embodiment, can, before passing through sub-cooled heat exchanger 30 and main heat exchanger 12, in expansion valve 63, make other liquid nitrogen stream 60 decompressions.
Thereby by carry out indirect heat exchange at the inner compressed and purifying air stream 10 with entering of main heat exchanger 12, heat the nitrogen product stream 64 acquisition nitrogen joint product that formed by nitrogen rich vapor overhead 23, also contribute to cooling-air stream 10 simultaneously.As shown in the figure, by the nitrogen enriched vapor stream 66 of taking out from main destilling tower 18 tops is separated into aforesaid two streams, and produce nitrogen product stream 64 and nitrogen enriched vapor stream 46.Yet, can from main destilling tower 18, take out individually nitrogen product stream 64 and nitrogen enriched vapor stream 46.It should be pointed out that because can import main destilling tower 18 using whole liquid nitrogen stream 50 as backflow, so can only form nitrogen joint product by the nitrogen product stream 64 through heating.
By taking out the residue oxygen enriched liquid stream 68 being formed by residue oxygen enriched liquid 56 and this conductance being entered to separation container 70, and produce oxygen joint product.In condenser 14, make the liquid phase stream 72 part evaporations that formed by liquid phase 74 produce two phase flow 76 to carry out indirect heat exchange by the compressed and purifying air stream 10 with entering, thus by compressed and partly condensation of air stream 10 purifying.In separation container inside, make the liquid distillate of two phase flow 76 separated with vapor fraction, with form vapor fraction with by the liquid phase 74 that produces of interpolation with the separated of stream and residue oxygen enriched liquid 68.Can utilize control valve (not shown) to regulate the operating pressure of container 70.The vapor phase flow 80 being comprised of vapor fraction 78 forms oxygen product and flows.Can optionally the discharge currents by valve 84 82 be collected as fluid product (or discharging evaporimeter as pollutant).Alternatively, can extract a part of stream 68 as fluid product and be delivered to suitable storage facility.
It should be pointed out that and can utilize the auxiliary destilling tower 34 that is positioned at the position that surpasses main destilling tower 18 height by remaining oxygen enriched liquid stream 68 pressurizations.Form thus the oxygen product through pressurization.Another substitutes is by means of the use of mechanical pump or pump the head of liquid producing in conjunction with the top by auxiliary destilling tower 34 is positioned to main destilling tower 18, by the pressurization of remaining oxygen enriched liquid stream.
As shown in the figure, condenser 14 plays thermal siphon.As the replacement device that is used to form oxygen product, separation container 70 can be built into and hold condenser 14.In this case, two phase flow will leave condenser and enters the inside of separation container 70.Yet, it is generally acknowledged, this illustrated embodiment has more cost benefit than above-mentioned layout.In addition, if the oxygen product that is greater than approximately 20% is used as to fluid product by discharge currents 82, condenser 14 can be reconstituted to once-through heat exchanger so and likely further save power consumption.In this layout, utilize pipeline that remaining oxygen enriched liquid stream 68 is directly delivered to condenser 14.Then, in phase separation container, by the separation of products of part evaporation and will there not be reflow stream, for example, be imported into the oxygen enriched liquid stream in condenser 14.
With reference to Fig. 2, show alternate embodiments of the present invention as air separation equipment 2.It should be pointed out that the element shown in Fig. 2 by tool with above with reference to Fig. 1, discuss identical description, this element shown in Fig. 2 will be used and reference number identical in Fig. 1; For not doing further discussion for purpose of brevity.Air separation equipment 2 is designed to allow contained nitrogen in larger mark air to be reclaimed as product particularly.This is to realize to the liquid nitrogen reflux of main destilling tower 18 by increasing.
In air separation equipment 2, after main heat exchanger 12 inside are cooled, the air stream of compressed and purifying 10 is imported to main destilling towers 20 and carries out rectifying, to produce nitrogen rich vapor overhead 23 and thick liquid oxygen bottoms 26'.After expansion valve 32 inside are depressurized, can optionally in sub-cooled unit 30', by thick liquid oxygen stream 28 ' sub-cooled and in auxiliary destilling tower 34 inside, carry out stripping.In the mode described in air separation equipment 1, in once-through heat exchanger 48 by the first nitrogen enriched vapor stream 46 condensations to produce the first liquid nitrogen stream 50 and remaining oxygen enriched liquid 56.After being depressurized in expansion valve 90, the gained residue oxygen enriched liquid stream 68 producing in auxiliary destilling tower 34 is imported in thermosyphon reboiler 86.Can and will remain oxygen enriched liquid, flow 68 part evaporations by carrying out indirect heat exchange with gaseous flow 92, described gaseous flow 92 can be consisted of the nitrogen rich vapor overhead 23 of main destilling tower 18.Gaseous flow 92 passes into the core 94 that is positioned at thermosyphon reboiler 86 housing 96 inside, to complete heat exchange.Gaseous flow 92 condensations are usingd and produced the condensate stream 98 be imported in main destilling tower 18 as a part for the backflow at above-mentioned tower.The whole liquid nitrogen streams that produce in once-through heat exchanger 48 50 are imported to main destilling tower 18 to reflux as tower.The segmentation condensation of this nitrogen rich vapor overhead will increase liquid nitrogen reflux, therefore increase the ability that air separation equipment 2 is produced nitrogen product.
As understandable, if discharge currents 106 has enough flows, can use other device (comprising once-through heat exchanger) that replaces thermosyphon reboiler 86.In addition, although not shown, replace nitrogen rich vapor, the conductance with the nitrogen concentration of the nitrogen concentration that is not less than air can be entered to the core 94 of thermosyphon reboiler 86.For example, can and in main heat exchanger 12, make this flow liquid by air stream compression.After this, can be imported the centre position of main destilling tower 18.Then, having the gaseous flow that flows roughly the same composition with this liquid can enter the core 94 of thermosyphon reboiler 86 and be condensed.Gained condensate stream is imported to the position of main destilling tower, in this position, the composition of the tower liquid of decline is identical with above-mentioned condensate liquid or approximate identical, or this condensate stream is imported to auxiliary destilling tower 34 to carry out stripping and the production of oxygen joint product.
The part evaporation of residue oxygen enriched liquid stream 68 forms vapor fraction and liquid distillate, and this vapor fraction and liquid distillate collect in housing as vapor fraction 100 and liquid phase 102.In main heat exchanger 12 inside, there is indirect heat exchange with the air stream of the compressed and purifying entering 10 in the vapor phase flow 104 being comprised of vapor fraction 100, so that heating steam flows 100 mutually, thereby produces oxygen product (" O 2") and contribute to the air stream 10 of cooling compressed and purifying.The discharge currents 106 being comprised of liquid phase 102 can be depressurized and be used as liquid oxygen product-collecting in valve 108.In this embodiment, optionally, can there is indirect heat exchange at the inner and thick liquid oxygen stream 28' of sub-cooled heat exchanger 30' in waste stream 62.Subsequently, at main heat exchanger 12 internal waste streams 62, also there are indirect heat exchange with the air stream 10 of compressed and purifying, to heat waste stream 62 and to help the air stream 10 of cooling compressed and purifying.Waste stream 62 can be recycled in the air entering.This can directly be mixed and heated afterwards or further after compression, complete by the air with entering in interchanger 12.As the situation in air separation equipment 1, by the compressed and purifying air stream 10 with entering, there is indirect heat exchange, and in main heat exchanger 12 inside, the nitrogen product stream being comprised of nitrogen rich vapor overhead 23 64 is heated, thereby also contribute to cooling compressed and purifying air stream 10.
See figures.1.and.2, by means of liquid nitrogen stream 110, to air separation equipment 1 or air separation equipment 2, freeze; Then liquid nitrogen stream 110 is imported into the top inlet 114 at the top that is positioned at main destilling tower 18 by flow control valve 112.Can from on-the-spot basin, obtain liquid nitrogen stream 110 and liquid nitrogen stream 110 can have high pressure or low pressure.The interpolation compensate for ambient heat leak of liquid nitrogen stream 110 and the warm end losses causing due to the operation of main heat exchanger 12.It should be pointed out that liquid can be flowed to 110 directly imports in a steam flow in the steam flow that enters heat exchanger 30' or 12.As understandable, before importing main destilling tower 18, can make the air that enters of a part expand.In this respect, after main heat exchanger 12 interior sections are cooling, can make compressed and air stream purifying of a part expand, then mix with waste gas streams 62.Another kind of may will be that distillation column system to main destilling tower 18 applies back pressure and can will assist in main heat exchanger 12 inside destilling tower 34 and waste stream 62 parts heating, expands and in the inner further heating of main heat exchanger 12 in turbo-expander.The use of turbo-expander can provide the possibility of taking out fluid product from Tower System.The a part of liquid nitrogen obtaining can be delivered to suitable storage facility from condenser 48 or 96.Another substitutes is liquid oxygen stream can be imported to remaining oxygen enriched liquid stream 68 or mix with this liquid stream 68, then imports in the housing 96 of thermosyphon reboiler 86.
With reference to Fig. 3, show the air separation equipment 1' of the alternate embodiments of air separation equipment 1 shown in pie graph 1.In air separation equipment 1, illustrated stand-by still 34 ' possesses stripping section 36a, and this stripping section 36a can possess as above with reference to the figure 1 mass transfer contact element 36 of describing.In this stripping section 36a inside, thick liquid oxygen stream 28 is carried out to stripping as mentioned above, rather than directly produce auxiliary overhead, but produce nitrogenous and steam oxygen.Stand-by still 34a also possesses the rectifying section 36b that is positioned at stripping section 36a top, and this rectifying section 36b is for this nitrogenous and steam oxygen is carried out to rectifying, recovery section oxygen thus, these oxygen otherwise just discharge from equipment in waste stream 62.The liquid nitrogen stream 60' that utilization is imported into stand-by still 34' top after with valve 63' decompression refluxes in this rectifying section.As understandable, can make identical modification to the equipment shown in Fig. 2.In this case, by be similar to the mode shown in Fig. 3 by stand-by still correct.In the situation that the embodiment of Fig. 2, by the condensate stream 98 of part for refluxing at stand-by still 34'.
As understandable, all expections be by otherwise the oxygen of the part that can lose in refuse is reclaimed to increase oxygen reclaims.Yet, the oxygen that must break increase reclaim with from otherwise by being used in, in the liquid nitrogen refluxing, taking out liquid nitrogen and so produce the balance between the fact of nitrogen main destilling tower.Any larger rectifying will be followed the flow of liquid nitrogen stream 60' to increase therefore and follow the decline that can utilize product nitrogen 64, because must maintain the reflux ratio of king-tower in order to maintain product nitrogen impurity.Mode more specifically in statement in this restriction is the performance of rectifying section 36b, and when performance in conjunction with stripping section 36a, the auxiliary overhead 38 in stand-by still 36 inside should contain the oxygen that is not less than 5.0 volume %.In order to reach this object, conventionally liquid nitrogen stream 60' and the flow-rate ratio that always can utilize nitrogen stream from tower 18 (flow 60 and 64 summation) should be between 0.1 and 0.4, and the ratio of the liquid/vapor in rectifying section 36b is 0.23 or less.
Although described the present invention with reference to preferred embodiment, just as the skilled person will appreciate, can make many variations, interpolation and omission under the prerequisite that does not deviate from the spirit and scope of the invention of stating in claims.

Claims (21)

1. separated air is to produce a method for oxygen and nitrogen joint product, and described method comprises:
The cooling compressed and aeriferous stream of bag purifying;
In main destilling tower inside, compressed and stream purifying are carried out to rectifying, to produce nitrogen rich vapor overhead and thick liquid oxygen;
By the auxiliary overhead that at least in part the thick liquid oxygen stream decompression being comprised of thick liquid oxygen is produced to oxygen enriched liquid and contains the oxygen that is not less than 5.0 volume % in auxiliary destilling tower inside, at the inner stripping gas with rising of described auxiliary destilling tower, described thick liquid oxygen stream is carried out stripping and by carrying out indirect heat exchange with the nitrogen enriched vapor stream being comprised of described nitrogen rich vapor overhead, described oxygen enriched liquid partly evaporated, produce thus liquid nitrogen stream, stripping gas and remaining oxygen enriched liquid;
With at least part of described liquid nitrogen stream, in described main destilling tower, reflux;
By making described remaining oxygen enriched liquid stream and the gaseous flow with the nitrogen concentration of the nitrogen concentration that is not less than air carry out indirect exchange heat, make the evaporation of described remaining oxygen enriched liquid stream part, and form oxygen-rich steam cut by described remaining oxygen enriched liquid;
By described vapor fraction, forming oxygen product flows; By described nitrogen rich vapor overhead, form nitrogen product stream; By described auxiliary overhead, form waste stream; With
Make described oxygen product stream, described nitrogen product stream and described waste stream and described stream compressed and purifying carry out indirect heat exchange.
2. the method for claim 1, wherein said auxiliary overhead is only to produce by described thick liquid oxygen stream being carried out to stripping in auxiliary destilling tower inside.
3. the method for claim 1, wherein refluxes in described main destilling tower with the described liquid nitrogen stream of part;
In the inside of auxiliary distillation exhausting section of column, carry out the stripping of described thick liquid oxygen stream;
In described auxiliary destilling tower inside, described thick liquid oxygen stream is carried out to the steam flow that stripping produces nitrogenous and oxygen; With
By being imported to described rectifying section, the described steam flow that contains nitrogen and oxygen, in the inside of described auxiliary destilling tower that is arranged in the rectifying section of the described auxiliary destilling tower above described stripping section, described nitrogenous and steam flow oxygen is carried out to rectifying, and with the described liquid nitrogen stream of another part, in described auxiliary destilling tower, therefore in described rectifying section, reflux, the oxygen improving thus in described residue oxygen enriched liquid inside reclaims.
4. the method for claim 1, wherein:
At oxygen enriched liquid described in described auxiliary destilling tower internal gathering; With
Oxygen enriched liquid stream and described nitrogen enriched vapor stream by making to be comprised of described oxygen enriched liquid partly evaporate described oxygen enriched liquid by once-through heat exchanger, so that the described remaining oxygen enriched liquid that forms described stripping gas and collect as the bottoms of described auxiliary destilling tower.
5. method as claimed in claim 4, wherein:
Described gaseous flow is compressed and stream purifying;
In condenser by the partly condensation of stream of described compressed and purifying;
Form in the following manner described oxygen-rich steam cut:
Described remaining oxygen enriched liquid stream is collected in separation container;
Liquid phase stream by forming in the inner liquid phase producing of described separation container is imported to described condenser, and in described condenser, by carrying out indirect heat exchange with described compressed and purified stream, described liquid phase stream is partly evaporated, from described liquid phase stream, produce two phase flow thus;
Described two phase flow is imported to described separation container and in the inside of described separation container, make the liquid phase of described two phase flow and vapor phase separation to form oxygen-rich steam cut, and described liquid phase is collected in described separation container together with described remaining oxygen enriched liquid stream; With
By give off the stream of described oxygen-rich steam cut from described separation container, and form described oxygen product stream.
6. method as claimed in claim 5, wherein said condenser is arranged in main destilling tower bottom zone the air of condensation is mixed with the liquid of the decline being produced by described rectifying, produces thus the thick liquid oxygen as the bottoms in described main destilling tower.
7. method as claimed in claim 6, wherein:
With the described liquid nitrogen stream of part, in described main destilling tower, reflux; With
Described waste stream and described thick liquid oxygen stream be exchanged heat indirectly, made before decompression described thick liquid oxygen stream sub-cooled.
8. method as claimed in claim 4, wherein:
Described gaseous flow is comprised of described nitrogen rich vapor overhead;
By by be rich in the stream decompression of liquid oxygen and make described remaining oxygen enriched liquid stream in thermosyphon reboiler inside by and carry out indirect heat exchange with described gaseous flow, and between described remaining oxygen enriched liquid stream and described gaseous flow exchanged heat indirectly, by the part of described residue oxygen enriched liquid stream, evaporate thus and produce described vapor fraction and the condensation by described air-flow produces condensate stream; With
Described condensate stream is imported to described main destilling tower as the backflow together with described liquid nitrogen stream.
9. method as claimed in claim 8 wherein made described waste stream and described thick liquid oxygen stream carry out indirect heat exchange before the decompression of described thick liquid oxygen stream, so that by described thick liquid oxygen stream sub-cooled.
10. the method for claim 1, wherein pressurizes described remaining oxygen enriched liquid stream so that also by the pressurization of described oxygen product stream.
11. the method for claim 1, wherein enter liquid nitrogen refrigerating conductance described main destilling tower to freeze.
12. 1 kinds for separating of air to produce the device of oxygen and nitrogen joint product, described device comprises:
Main heat exchanger, it is configured to the cooling compressed and aeriferous stream of bag purifying;
Main destilling tower, it is configured to described compressed and stream purifying to carry out rectifying to produce nitrogen rich vapor overhead and thick liquid oxygen;
Auxiliary destilling tower, it is connected to described main destilling tower and is configured to and with the stripping gas rising, the thick liquid oxygen stream being comprised of described thick liquid oxygen is carried out to stripping in the inside of described auxiliary destilling tower, and at least in part due to the auxiliary overhead that the stripping of described thick liquid oxygen stream is produced to oxygen enriched liquid and contain the oxygen that is not less than 5.0 volume %;
Expansion valve, its between described main destilling tower and auxiliary destilling tower in case before being imported into described auxiliary destilling tower by described thick liquid oxygen stream decompression;
Device, it partly evaporates described oxygen enriched liquid by carrying out indirect heat exchange with the nitrogen enriched vapor stream being comprised of described nitrogen rich vapor overhead, produces thus liquid nitrogen stream, stripping gas and residue oxygen enriched liquid;
Described oxygen enriched liquid part vaporising device is connected to described main destilling tower, makes to reflux in described main destilling tower with at least part of described liquid nitrogen stream;
Described main heat exchanger is connected to described main destilling tower and described auxiliary destilling tower, so that the nitrogen product stream being comprised of described nitrogen rich vapor overhead and by the air stream of the formed waste stream of auxiliary overhead of described auxiliary destilling tower and described compressed and purifying exchanged heat indirectly;
Device, it is for making described remaining oxygen enriched liquid stream carry out exchanged heat indirectly with the gaseous flow with the nitrogen concentration of the nitrogen concentration that is not less than air, to make the evaporation of described remaining oxygen enriched liquid stream part; And device, it for forming oxygen-rich steam cut by described residue oxygen enriched liquid stream after by part evaporation; With
Described main heat exchanger is connected to described oxygen-rich steam cut and forms device, described main destilling tower and described auxiliary destilling tower, make by the oxygen product stream of described oxygen-rich steam fractional composition, the nitrogen product stream being formed by described nitrogen rich vapor overhead and the waste stream that formed by the auxiliary overhead of described auxiliary destilling tower in described main heat exchanger inside by and carry out indirect heat exchange with described stream compressed and purifying.
13. devices as claimed in claim 12, wherein said stand-by still only possesses wherein described thick liquid oxygen stream is carried out to steam stripped stripping section.
14. devices as claimed in claim 12, wherein:
Described stand-by still has stripping section and is positioned at the rectifying section of described stripping section top;
In the inside of auxiliary distillation exhausting section of column, carry out the stripping of described thick liquid oxygen stream, and in described stripping section, produce nitrogenous and steam flow oxygen, described nitrogenous and steam flow oxygen enters described rectifying section to described nitrogenous and steam flow oxygen is carried out to rectifying, and the oxygen improving thus in described residue oxygen enriched liquid inside reclaims;
Described oxygen enriched liquid part vaporising device is connected to described main destilling tower, to reflux in described main destilling tower with the described liquid nitrogen stream of part, and be also connected to described auxiliary destilling tower to therefore reflux in described auxiliary destilling tower with the described liquid nitrogen stream of another part in described rectifying section; With
Another expansion valve is between described oxygen enriched liquid part vaporising device and described auxiliary destilling tower, to the pressure of the liquid nitrogen stream of described another part is reduced to the pressure of described auxiliary destilling tower.
15. devices as claimed in claim 12, wherein:
Described auxiliary destilling tower has for collecting the device of described oxygen enriched liquid;
Described oxygen enriched liquid part vaporising device is once-through heat exchanger, described once-through heat exchanger be connected to auxiliary destilling tower and described oxygen enriched liquid gathering-device in case by the oxygen enriched liquid stream that formed by described oxygen enriched liquid pass through described oxygen enriched liquid is evaporated at described once-through heat exchanger interior section, and described remaining oxygen enriched liquid is collected as the bottoms of described auxiliary destilling tower; With
Described main destilling tower is connected to described once-through heat exchanger, so as in described once-through heat exchanger inside by described nitrogen enriched vapor stream condensation.
16. devices as claimed in claim 15, wherein:
Described gaseous flow is the air stream of described compressed and purifying;
It is condenser and separation container that described remaining oxygen enriched liquid heat-exchange device and described oxygen-rich steam cut form device, and described condenser is connected to described main heat exchanger, so that by the partly condensation of stream of described compressed and purifying;
Described separation container is connected to described auxiliary destilling tower, so that described remaining oxygen enriched liquid stream collects in described separation container;
Described separation container is connected to described condenser so that by making the liquid phase stream forming in the inner liquid phase producing of described separation container partly evaporate in described condenser, to produce, be imported into the two phase flow in described separation container, in the inside of described separation container, make the liquid phase of described two phase flow and vapor phase separation to form described oxygen-rich steam cut and described liquid phase; With
Described main heat exchanger is connected to described separation container and flows to form described oxygen product by described oxygen-rich steam cut.
17. devices as claimed in claim 16, the bottom zone that wherein said condenser is arranged in described main destilling tower make through condensation air with by described compressed and stream purifying being carried out to the liquid of the decline that rectifying produces, mix, to produce the thick liquid oxygen as bottoms in described main destilling tower.
18. devices as claimed in claim 17, wherein:
Described once-through heat exchanger is connected to described main destilling tower to reflux in described main destilling tower with the described liquid nitrogen stream of part; With
Sub-cooled heat exchanger is connected to described once-through heat exchanger, described auxiliary destilling tower and described expansion valve, so that described waste stream and described thick liquid oxygen stream be exchanged heat indirectly in the inside of described sub-cooled heat exchanger, and before by described expansion valve by described thick liquid oxygen stream sub-cooled.
19. devices as claimed in claim 15, wherein:
Described gaseous flow is comprised of described nitrogen rich vapor;
It is the thermosyphon reboiler with housing that described remaining oxygen enriched liquid stream heat-exchange device and described oxygen-rich steam cut form device;
Described housing is connected to described stand-by still to receive described remaining oxygen enriched liquid stream;
Another expansion valve is between described housing and described stand-by still, so that by the decompression of described remaining oxygen enriched liquid stream;
Described thermosyphon reboiler is connected to described main destilling tower to receive described gaseous flow, by making described gaseous flow condensation with the indirect heat exchange of described residue oxygen enriched liquid stream, in the inside of described housing, form thus described oxygen-rich steam cut and condensate stream is discharged into described main destilling tower as the backflow together with described liquid nitrogen stream thus; With
Described main heat exchanger is connected to described housing, described main destilling tower and described auxiliary destilling tower and makes by the formed oxygen product stream of described vapor fraction, by the formed nitrogen product stream of described nitrogen rich vapor overhead, by the formed waste stream of auxiliary overhead from producing described auxiliary destilling tower, in the inside of described main heat exchanger, passed through, and carries out indirect heat exchange with compressed and stream purifying.
20. devices as claimed in claim 19, wherein sub-cooled heat exchanger is between described auxiliary destilling tower, described main destilling tower and described main heat exchanger, to heat described waste stream and described thick liquid oxygen stream before described waste stream before the decompression of described thick liquid oxygen stream and in described main heat exchanger, carries out indirect heat exchange.
21. devices as claimed in claim 12, wherein said main destilling tower has the top inlet that flows to freeze for importing liquid nitrogen refrigerating.
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BR112014012911A2 (en) 2017-06-13

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