CN101285640A - Nitrogen production method and apparatus - Google Patents
Nitrogen production method and apparatus Download PDFInfo
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- CN101285640A CN101285640A CNA200810109272XA CN200810109272A CN101285640A CN 101285640 A CN101285640 A CN 101285640A CN A200810109272X A CNA200810109272X A CN A200810109272XA CN 200810109272 A CN200810109272 A CN 200810109272A CN 101285640 A CN101285640 A CN 101285640A
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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
- F25J3/044—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 single pressure main column system only
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/72—Refluxing the column with at least a part of the totally condensed overhead gas
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
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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
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/52—Processes or apparatus involving steps for increasing the pressure of gaseous process streams the fluid being oxygen enriched compared to air, e.g. "crude 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude 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
- 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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- 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
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/52—One fluid being oxygen enriched compared to air, e.g. "crude oxygen"
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- Engineering & Computer Science (AREA)
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- General Engineering & Computer Science (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Method and apparatus for distilling nitrogen from a gaseous mixture containing nitrogen and oxygen. Oxygen-enriched bottoms liquid is partially vaporized within a first heat exchanger to condense part of the column overhead to produce reflux. Thereafter, the partially vaporized oxygen-enriched liquid is phase separated. A second oxygen-enriched liquid stream composed of at least part of the liquid phase is used to substantially condense all or part of the vapor stream derived from said phase separation, thereby to form a nitrogen-rich liquid stream. At least part of the nitrogen-rich liquid stream is reintroduced into the column to increase nitrogen recovery. The second oxygen-enriched liquid stream is then used to condense a second part of the reflux for the column.
Description
Technical field
The present invention relates to wherein evaporate the oxygen enriched liquid that is made of tower bottom distillate by cryogenic rectification separating gas mixture in rectifying column with the method and apparatus of production nitrogen product, the overhead fraction that condensation simultaneously contains nitrogen refluxes to form rectifying column.More particularly, the present invention relates to a kind of like this method and apparatus, wherein oxygen enriched liquid is by continuous evaporation, and is cooled mutually and introduced subsequently in the tower to improve rate of recovery of nitrogen again by the nitrogen rich vapor that the oxygen enriched liquid continuous evaporation produces.
Background technology
Can be by cryogenic rectification from comprising the admixture of gas of nitrogen and oxygen, separation of nitrogen in the air for example.Typically, compression and the air fluid that purified are cooled to the temperature of suitable its rectifying, subsequently oxygen enrichment cut at the bottom of rectifying generation cat head nitrogen rich vapor and the tower in rectifying column.Backflow by some nitrogen rich vapors generation towers of condensation.This condensation is finished by a nitrogen rich vapor fluid and an oxygen enrichment tower bottom distillate stream strand indirect heat exchange.Partially liq can be used as product.
The final evaporation of oxygen enrichment tower bottom product produces the waste streams thigh.This waste streams thigh and nitrogen product stream thigh by main heat exchanger with cooling compression of charging and the air that purified.Heat waste streams thigh, waste streams thigh by turbo-expander and heating waste streams thigh in main heat exchanger subsequently by part in main heat exchanger, refrigeration can be provided.
Usually, the condenser performance that is used for oxygen enriched liquid and nitrogen rich vapor heat exchange is inefficient.There is excessive temperature difference between the oxygen enriched liquid fluid of evaporation and the cat head nitrogen cut of cooling.Thereby most of because of the heat exchange at condenser, this method has disappeared and has consumed extra work done during compression.In addition, there is excessive component gradient near at the bottom of the rectifying Tata.Especially, occurring fast in the level seldom, composition changes.Rapid composition like this changes corresponding to a large amount of thermodynamics irreversibility that changes lost work into.In the prior art, a large amount of effort mainly concentrate on the condenser operation and tower reclaims.
US4867773 and US4872893 have described similar method in detail, relate to single tower nitrogen rectificating method, and wherein the oxygen enrichment tower bottom distillate to the small part evaporation is heated, compresses and is recycled in the tower.Reflux fluid is with the position charging lower than feeding air.Improved effect make overhead condenser more valid function to increase nitrogen recycling.
US4883519 has illustrated another kind of single tower nitrogen rectificating method, and wherein overhead fraction nitrogen is by two heat exchanger condensations.In this method, oxygen enrichment tower bottom distillate fluid pressure to the first pressure and part evaporation.The steam that produces is recycled to main air compressor.Remaining oxygen enriched liquid further reduces pressure and introduces fully evaporation in the second low pressure heat exchanger.The steam introducing turbo-expander that generates to small part is used for condensation production.
US4927441 discloses another kind of single tower nitrogen method, and it is similar among the US4883519 disclosed.In this was provided with, the oxygen enrichment tower bottom distillate was decompressed to first pressure and introduces separation container subsequently, and it contains the little mass transfer part that comprises as the mass transfer component of filler.This mass transfer column partly is used for the oxygen of further enrichment fluid before fluid pressure and introducing second heat exchanger.The advantage of this device is to be created in overhead fraction that mass transfer partly produces and air and constitutes very approachingly, therefore can utilize by main air compressor again, and constitute losses by mixture not accordingly.
US5711167 discloses a kind of single tower nitrogen method, and wherein two overhead condensers are used for producing by the oxygen enriched liquid continuous evaporation backflow of rectifying column.In the evaporation of the oxygen enriched liquid first that carries out in one of two overhead condensers, the steam of generation is compressed in refrigeration compressor and draws back rectifier bottoms.The oxygen enrichment discarded object that the oxygen enriched liquid that carries out in second condenser part evaporation for the second time produces heats before discharging and expands.At least the shaft work of demi-inflation is introduced refrigerant compression.
US5899093 has described a kind of method in detail, and wherein the oxygen enrichment tower bottom distillate is at first partly reduced pressure and introduces rectifying type condenser.The oxygen enrichment tower bottom distillate that results from the condenser is isolated nitrogen-rich gas, and by in air compressor, carry out gas compress back and forth contracture from nitrogen-rich gas.The residual fluid of oxygen enrichment further reduces pressure and is used for the extra section of condensation from the overhead fraction nitrogen of tower more.The residual fluid of oxygen enrichment further reduces pressure and is used for the extra section of condensation from the overhead fraction nitrogen of tower more.The nitrogen cut that first-selected part evaporation obtains is recycled to gas compressor, arrives tower subsequently.
US5934106 and US5868006 disclose a kind of single tower nitrogen gas generator, and wherein overhead fraction nitrogen is by two fluid condensations from Tower System.The liquid fluid evaporation of the first rich nitrogen class air also recompresses back in the tower.The second oxygen enrichment tower bottom distillate fluid proposes from tower and also is evaporated.Second evaporated fraction is heated and expands subsequently.The shaft work that expansion work provides the refrigerant compression of first circulation of fluid to need.
What discuss is, the present invention relates to contain the cryogenic rectification of gas in rectifying column of oxygen and nitrogen by air or other, reclaim the method for nitrogen rich vapor, wherein the nitrogen-rich liquid condensate that produces in the oxygen enriched liquid fluid continuous evaporation that is made of the liquid column bottoms cut to small part is introduced into rectifying column, generates with the steam that increases nitrogen rich vapor in energy efficiency and cost efficiency mode.
Summary of the invention
The invention provides a kind of separation and comprise that the admixture of gas of nitrogen and oxygen is to generate the method for nitrogen product.According to this method, introduce rectifying column to generate cat head nitrogen rich vapor and oxygen enriched liquid tower bottom distillate by gaseous fluid purification, that compress and cool off that admixture of gas constitutes.The first oxygen enriched liquid fluid pressure that constitutes by the oxygen enriched liquid tower bottom distillate to small part and subsequently in the first heat exchanger vaporized in part.Vapor phase breaks away from from the liquid phase that is formed by the evaporation of the first oxygen enriched liquid fluid section.The second oxygen enriched liquid fluid pressure that constitutes by liquid phase to small part and subsequently by the vapor phase fluid that constitutes by vapor phase with at least a portion in the second heat exchanger indirect heat exchange and the part evaporation.This abundant condensing gas phase fluid is to form the nitrogen-rich liquid fluid.
First's condensation in first heat exchanger of the cat head nitrogen-rich stream that constitutes by the cat head nitrogen rich vapor, the condensation in the 3rd heat exchanger of the second portion of cat head nitrogen-rich stream.Indirect heat exchange carries out by evaporating afterwards with second oxygen-rich fluid in its part in the condensation of the second portion of cat head nitrogen-rich stream, thereby further evaporates second oxygen-rich fluid.To the condensation of small part cat head nitrogen-rich stream, get back to rectifying column as backflow.
To small part nitrogen-rich liquid fluid subsequently purified, the compression and the cooling fluid above introduce rectifying column.Product nitrogen fluid results from the nitrogen rich vapor part.
The first oxygen enriched liquid fluid can by with the nitrogen product fluid and by the second oxygen enriched liquid fluid further the discarded fluid that constitute of the vapor fraction after the evaporation carry out indirect heat exchange and by cold excessively.If compression that is made of admixture of gas and the fluid that purified can be by crossing the discarded fluid after cold with nitrogen product fluid and oxygen-rich fluid and the second portion nitrogen rich vapor fluid indirect heat exchange before its compression that exists cools off.Thereby compression and the fluid cooling that purified are formed up to fluid that small part purified, that compress and cool off.
In a specific embodiment of the present invention, the first of vapor phase fluid can be in second heat exchanger fully condensation is forming the nitrogen-rich liquid fluid, and the second portion of gaseous fluid can and be recycled to rectifying column by warm (warm), compression and cooling.Cool off and recycle by after warm and compression, the second portion of vapor phase fluid and compression and the fluid that purified being combined to finish with the compression of formation merging and the fluid that purified.In this embodiment, the compression of merging and the fluid that purified are by the second portion cooling of nitrogen product fluid, discarded fluid and nitrogen rich vapor steam flow.Similarly, the second portion of vapor phase fluid cools off and recycles back rectifying column by uniting with compression and the fluid that purified.
Preferably, if the nitrogen rich vapor fluid of discarded fluid and nitrogen product fluid and existence is before its compression, all with the fluid indirect heat exchange in main heat exchanger that compresses and purify.Discarded fluid can be in main heat exchanger the warm and acting of expanding subsequently of part produce and discharge fluid.Discharge fluid and introduce main heat exchanger and fully warm again with the refrigeration low-temperature distillation process.It should be noted that herein and the term that uses in the claim " part is warm " means discarded fluid and is warmed to temperature between main heat exchanger hot junction and cold junction temperature.Herein and the term that uses in the claim " warm fully " mean the temperature that is warmed to the main heat exchanger hot junction fully.
The pressure of nitrogen-rich liquid fluid can be regulated after abundant condensation and before introducing rectifying column.This adjusting can be finished by mechanical pumping nitrogen-rich liquid fluid after the abundant condensation or expansion nitrogen-rich liquid fluid.
On the other hand, the invention provides a kind of separation and comprise that the admixture of gas of nitrogen and oxygen is to generate the device of nitrogen product.By this aspect of the present invention, rectifying column is connected fluid purification, that compress and cool off that is made of admixture of gas with rectifying, generation cat head nitrogen rich vapor and oxygen enriched liquid tower bottom distillate with main heat exchanger.
First valve is used to reduce pressure and comprises first oxygen-rich fluid to small part oxygen enriched liquid tower bottom distillate.First heat exchanger is connected in first valve and evaporates the first oxygen enriched liquid fluid with part, and phase separator is connected in first heat exchanger to separate gas phase the liquid phase of partly evaporating formation from first oxygen-rich fluid.Second valve is connected in phase separator and comprises the second oxygen enriched liquid fluid of Partial Liquid Phase at least with decompression, and second heat exchanger is connected in second valve and phase separator, with by part is evaporated the second oxygen enriched liquid fluid with partly evaporating the vapor phase fluid indirect heat exchange that the vapor phase that formed constitutes to small part by first oxygen-rich fluid.This abundant condensation the vapor phase fluid to produce the nitrogen-rich liquid fluid.The 3rd heat exchanger and the second heat exchanger serial operation are with the further evaporation second oxygen enriched liquid fluid.
Rectifying column be connected in first heat exchanger and the 3rd heat exchanger with condensation by the cat head nitrogen rich vapor constitute to small part cat head nitrogen-rich stream, and near small part cat head nitrogen-rich stream sends back to rectifying column as backflow after condensation.
Second heat exchanger is connected in rectifying column and enters rectifying column to guide to small part nitrogen-rich liquid fluid above the fluid that purified, compress and cool off.Be provided for extracting the equipment of the product nitrogen fluid that is formed at part cat head nitrogen rich vapor.
In a specific embodiment of the present invention, compression that main heat exchanger is made of admixture of gas with cooling and the fluid that purified can be provided, thereby form purified, compress also cooling fluid.In embodiment optionally, second heat exchanger can be connected in phase separator, make the first of vapor phase fluid in second heat exchanger fully condensation to form the nitrogen-rich liquid fluid.Compressor can link to each other with the phase separator fluid, and is connected in main heat exchanger, and the second portion that main heat exchanger can be designed such that the vapor phase fluid is warm and compress in compressor in main heat exchanger.Main heat exchanger among this selectivity embodiment also links to each other with compressor fluid with compression and the fluid that purified simultaneously, makes second portion and the compression of vapor phase fluid and the fluid that purified combine with the compression of formation combination and the fluid that purified.Among this embodiment, compression and the fluid that purified cool off the fluid that purified, compress and cool off to form in main heat exchanger.
Subcooler can be connected in rectifying column, makes the oxygen enriched liquid fluid of winning by with the nitrogen product fluid with by the further discarded fluid indirect heat exchange that constitutes of the vapor fraction after the evaporation and cold excessively of the second oxygen enriched liquid fluid.Main heat exchanger also is connected in subcooler and is designed such that the air fluid that compresses and purified is by crossing cold discarded fluid indirect heat exchange cooling afterwards with the nitrogen product fluid and first oxygen-rich fluid.If exist, the second portion of gaseous fluid also is used to cool off the compression of combination and the air fluid that purified.
Preferably, main heat exchanger can be designed such that also discarded fluid part in main heat exchanger is warm, and the discharge fluid is warm fully in main heat exchanger, to cool off this device.Decompressor is connected in main heat exchanger and makes the acting of expanding of the discarded fluid of part after warm in decompressor, with generation discharge fluid.
Pump can be put between second heat exchanger and the rectifying column, with pressurization nitrogen-rich liquid fluid after abundant condensation and before entering rectifying column.Optionally, the 3rd valve can be put between second heat exchanger and the rectifying column, to reduce the pressure of nitrogen-rich liquid fluid after abundant condensation with before entering rectifying column.The selection of pump or valve will be depended on the gravity head that the difference in height between second condenser and the nitrogen-rich liquid feed entrance point produces.
Clearly, nitrogen-rich liquid helps increasing the generation of nitrogen rich vapor to the backflow of tower in the description of method and apparatus of the present invention two aspects.This also reduced component at the bottom of the tower variation so that operating line more near the vapor liquid equilibrium curve, thereby produce higher efficient.This has reduced to be converted into the lost work that reduces compression requirements.Thereby the indirect heat exchange that is used for oxygen enriched liquid fluid that tower refluxes and nitrogen rich vapor can be finished than prior art is more effective by the recording equipment temperature difference that three grades of method of evaporating reduce the indirect heat exchange fluid.This obtains than the more efficient methods of finishing in the prior art.
Description of drawings
The specification established right requires clearly to have pointed out its subject matter of an invention that the applicant thinks, believes that the present invention and accompanying drawing connect will better be understood, wherein:
Fig. 1 is the schematic process chart that can be used for carrying out the device of the method among the present invention; And
Fig. 2 is the selectivity embodiment of Fig. 1.
Describe in detail
As shown in Figure 1, represented to be used for carrying out the device 1 of method of the present invention.
Comprise compression that nitrogen and oxygen constitutes and the fluid 10 that purified, air for example, cooling and is introduced rectifying column 14 subsequently and is used for oxygen separation and nitrogen forming the fluid 13 that purified, compress and cool off in main heat exchanger 12.In the rectifying column 14, the fluid 13 that purified, compress and cool off is distillated and is separated into oxygen enriched liquid tower bottom distillate 16 and cat head nitrogen rich vapor 18.The product fluid 20 that is made of nitrogen rich vapor 18 can be warm fully in main heat exchanger 12, and the cooling press fluid 10 that contracts and purified.
Rectifying column 14 comprises the mass transfer contact component, as is usually placed in the territory, tower base area 22 and the structured packing or the column plate that are positioned at the remaining area 24 of 22 tops, territory, tower base area of rectifying column 14.Typically, rectifying column 14 is in the approximately extremely approximately pressure limit operation of 12bar absolute pressure of 5bar.
Compression and fluid 10 unit operations that can be finished by additive method or that prior art is known that purified finally generate, also can utilize compressor and preliminary clearning unit to generate, described preliminary clearning unit use adsorbents adsorb water, carbon dioxide and can be in chilling process the hydrocarbon of condensation or the potentially dangerous that gathers.Can recognize that compressor can be used for being connected with the present invention with clean unit.
Compression and the fluid 10 that purified are introduced rectifying column 14 in about saturation temperature, and its introducing begins to form the gas phase of the rising of being rich in nitrogen all the time to form cat head nitrogen rich vapor 18.The cat head nitrogen-rich stream 26 that is made of the cat head nitrogen rich vapor proposes and is divided into and replenishes cat head nitrogen-rich stream 28 and nitrogen product fluid 20 from rectifying column 14.Yet be appreciated that nitrogen product fluid 20 can separate proposition from rectifying column 14.With what come into question, additional cat head nitrogen-rich stream 28 condensations produce the reflux fluid 29 of introducing rectifying column 14, contact also with the vapor phase that rises with formation and are rich in the liquid phase of the decline of oxygen all the time, form the oxygen enriched liquid 16 of tower bottom distillate when it descends.
Selectively cold excessively in crossing cold heat exchanger 32 by the first oxygen enriched liquid fluid 30 that the oxygen enriched liquid tower bottom distillate constitutes.The subcooled liquid pressure that produces is reduced by first valve 34.The first oxygen enriched liquid fluid 30 by first valve 34 is subsequently in first heat exchanger, 36 vaporized in part, to form two-phase fluid 38.Liquid and gas in the two-phase fluid 38 are separated into liquid phase 42 and gas phase 44 in phase separator 40.It should be noted that the oxygen enriched liquid fluid 30 by first heat exchanger 36 can typically have the vapor fraction between about 10% to about 40%, more preferably about 30%.
The second oxygen enriched liquid fluid 46 that comprises liquid phase 42 utilizes 48 decompressions of second valve, and subsequently in second heat exchanger, 50 vaporized in part.Pressure drop by second valve 48 is usually located at about 1.0 in the 1.5bar specification limit.What introduce second heat exchanger 50 equally is the gaseous fluid 52 that is made of with the gas phase 44 that forms nitrogen-rich liquid fluid 54 abundant condensation.Herein and the term that uses in the claim " fully condensation " mean fluid and have the liquid distillate that surpasses about 95% volume usually.And, it should be noted that the typical component of this nitrogen-rich liquid fluid is the nitrogen of 75 to 90% scopes.
The second oxygen enriched liquid fluid 46 after second heat exchanger, 50 vaporized in part is introduced the 3rd heat exchanger 56 subsequently, its thermal siphon operation that is expressed as nature is with the further evaporation second oxygen enriched liquid fluid 46, thereby produce the vapor fraction shown in the Reference numeral 58, it is discharged as discarded fluid 60.After heat exchanger 50 vaporized in part, the vapor fraction of the second oxygen enriched liquid fluid 46 is about 40% to about 60% scope, and is preferred, and about 45% to about 50%.
The condensation in first heat exchanger 36 of the first 62 of cat head nitrogen-rich stream 28, second portion 64 condensation in the 3rd heat exchanger 56 produces liquid fluid 66.Condenses fluid 66 to the small part combination is got back to rectifying column 14 as reflux fluid 29.Selectable product liquid fluid 68 also can extract and introduce the suitable containers (not shown).
Intelligible, first heat exchanger, 36, the second heat exchangers 50 and the 3rd heat exchanger 56 are generally the aluminium heater of brazing.Can use other heat exchanger types, for example the package type.If used the aluminium heater of brazing, first heat exchanger 36 and the 3rd heat exchanger 56 can be incorporated into separate modular.And any amount of heat exchanger circulation configuration all can be used.Heat exchanger can be as shown in the figure once by evaporimeter, perhaps can be designed to circulating evaporator.For example, all heat exchangers can be designed to the thermal siphon of nature and pump cyclical patterns.Intelligible, the heat exchanger 56 that is included in the container 70 that is connected with rectifying column 14 is the atural beat siphons by the guiding of gravity hydraulic head of boiling fluid.
It should be noted that the distribution of two-phase fluid in aluminium heater requires separating liquid and steam-gas inlet to distribute passage usually.In order to promote this distribution, the two-phase fluid 46 that enters the first oxygen enriched liquid fluid 30 of first heat exchanger 36 and enter second heat exchanger 50 can be separated.In addition, compression and the fluid that purified 10 are as the liquid and gas fluid introducing rectifying column 14 of compression and the fluid 10 partial condensations generation that purified.In another kind changed, first heat exchanger 36 and second heat exchanger 50 can be used for the purpose of cold other fluids, as the fluid before sending to storage 68.
Nitrogen-rich liquid fluid 54 is introduced rectifying column 14 above fluid 10 positions of compressing and purifying.This has increased the generation of nitrogen rich vapor and has reduced the composition gradient of rectifying column 14 bottom sections.Can recognize that the nitrogen content in the condensed fluid 54 will be higher than the content in the oxygen enriched liquid 16, thereby its higher position at rectifying column 14 is introduced.It should be noted that, be not that all nitrogen-rich liquid fluids 54 all need to enter rectifying column 14.The fluid 54 of part can be used for combining with fluid 10, evaporates also warm and/or recycles or introduce container 70 with the control heat exchanger.
For nitrogen-rich liquid fluid 54 is introduced rectifying column 14, in most cases, need the pressure adjustment to pass through equipment 72 condensed fluid 54.For example, enter the pressure of liquid fluid 54 of rectifying column 14 when too low, equipment 72 can be pump.If the use pump helps using container that extra liquid residence time is provided.This container preferably uses little steam to discharge line (can be connected in discarded fluid in case of necessity).Optionally, if make that the hydrostatic head of condensed fluid 54 is enough because the component in the ice chest is placed, equipment 72 can simply be valve.
As mentioned above, the first oxygen enriched liquid fluid 30 is cold excessively in sub-cooling unit 32, and it can be the aluminium heater of brazing, in fact can be the part of heat exchanger 12.The first oxygen enriched liquid fluid 30 is by the warm discarded fluid 60 of part and nitrogen product fluid 20 and cold excessively.After warm by part, discarded fluid 60 and nitrogen product fluid 20 are introduced compression that main heat exchangers 12 enter with cooling and the fluid 10 that purified.
The discarded fluid 60 of discharging from shell 70 typically can have about absolute pressure of 2 to about 7bar.In an illustrated embodiment, device 1 cools off by the warm discarded fluid 60 of part in main heat exchanger 12, discharge fluid 78 to form part warmed fluid 74 and in turbo-expander 76, to expand subsequently to produce, this fluid 78 is warmed to fully near environment temperature and pressure in main heat exchanger 12, thus cooling device 1.The shaft work that expands can give generator and be used for compressed air, nitrogen or discarded fluid 60 by warm oil brake expansion or before consuming.It should be noted that, but fluid 74 bypasses of part are by turbine 76 and use valve introduce to discharge fluid 78.The present invention has other cooling types, comprise, external source or even prior art in the air expander of explaining.
As shown in Figure 2, nitrogen-rich liquid fluid 54 is made of the 52a of first of vapor phase fluid 52.The second portion 52b of vapor phase fluid 52 is by main heat exchanger 12 ' and compression in compressor 80 subsequently.In main heat exchanger 12 ' fully warm after, the second portion 52b of vapor phase fluid 52 can be subsequently combine compression of making up with formation and the fluid 11 that purified with compression and the fluid 10 that purified.After the cooling, the fluid 13 ' purification of generation, that compress and cool off is introduced rectifying column 14 in main heat exchanger 12 '.It should be noted that similarly configuration can relate to the fluid that part is warm 74 separately, returns the bottom of another part to rectifying column 14 so that segment fluid flow compresses.Another realizes that the optionally scheme of this purpose is that the second portion 52b of the split tunnel recirculation vapor phase fluid 52 by main heat exchanger 12 ' gets back to rectifying column 14.And discarded fluid 60 can be introduced another rectifying zone or optionally can be by warm, compression and subsequently as the charging of similar procedure.
The present invention can be used for the combination of rectifying column of the similar described function of formation of any amount.For example, rectifying column 14 can use auxiliary reboiler with further increase and recirculation.In this device, extra air and nitrogen fluid can be compressed to elevated pressures and condensation in reboiler, thereby extra steam flow is provided.
And rectifying column 14 can use the combination of accumulation and structured packing.Rectifying column 14 can be divided into a plurality of zones.As be known in the art, " reflux pump " can be used for that tower liquid is imported the tower neutralization and draws from the tower zone.In this, equipment 72 can be the mechanical pump as reflux pump and pressure control equipment.
In another possible embodiment of the present invention, other oxygen-rich fluids can extract and add replenishing with to the temperature control of first heat exchanger 36, second heat exchanger 50 and the 3rd heat exchanger 56 or reduce size as oxygen enriched liquid fluid 30 from rectifying column 14.
Also may utilize some aspect of directly not using heat exchanger 12 or 12 ' (or aforesaid compression and preliminary clearning equipment) among the present invention.For example, Chang Gui single tower nitrogen gas generator can be used for generating fluid purification, that compress and cool off.This fluid can be by obtaining from extracting oneself the oxygen enrichment tower bottom distillate with the evaporation of the condenser of single tower nitrogen gas generator associating.In this, single tower nitrogen gas generator is preferably operated in 10 to about 20bar pressure limit.Rectifying column 14 can be by aforesaid operations.Nitrogen product and discarded fluid can by with as described in Figure 1 similarly mode pass through main heat exchanger.
Though the present invention is described with reference to preferred embodiment, to those skilled in the art, changes in a large number and increase in the spirit and scope of the present invention that in the claim of not leaving as present unexamined, to illustrate and make.
Claims (17)
1. a separation comprises the method for the admixture of gas of nitrogen and oxygen with the generation nitrogen product, and described method comprises:
The gaseous fluid that purified, compress and cool off is introduced rectifying column to generate cat head nitrogen rich vapor and oxygen enriched liquid tower bottom distillate;
Decompression comprises the first oxygen enriched liquid fluid to small part oxygen enriched liquid tower bottom distillate, at the first heat exchanger vaporized in part, the first oxygen enriched liquid fluid, from the liquid phase that the evaporation of the first oxygen enriched liquid fluid section forms, separate vapor phase, decompression comprises the second oxygen enriched liquid fluid of Partial Liquid Phase at least and by coming part to evaporate the second oxygen enriched liquid fluid with the liquid phase fluid indirect heat exchange that is made of liquid phase to small part in second heat exchanger, thereby fully is condensed to small part vapor phase fluid to form the nitrogen-rich liquid fluid;
First's condensation in first heat exchanger of the cat head nitrogen-rich stream that constitutes by the cat head nitrogen rich vapor, indirect heat exchange carries out condensation to the second portion of cat head nitrogen-rich stream by evaporating afterwards with second oxygen-rich fluid in its part in the 3rd heat exchanger, thereby further evaporate second oxygen-rich fluid, the cat head nitrogen-rich stream of partial condensation is got back to rectifying column as backflow at least;
To small part nitrogen-rich liquid fluid purified, the compression and the cooling liquid fluid above introduce rectifying column;
Part by the cat head nitrogen rich vapor generates product nitrogen fluid.
2. the method for claim 1 further comprises:
By with the nitrogen product fluid with comprise the further discarded fluid indirect heat exchange of the evaporated fraction after the evaporation of the second oxygen enriched liquid fluid, thereby cross the cold first oxygen enriched liquid fluid; And
By crossing cold discarded fluid indirect heat exchange afterwards with nitrogen product fluid and oxygen-rich fluid, thereby compression that cooling is made of admixture of gas and the fluid that purified, thereby compression and the fluid that purified are formed up to fluid that small part purified, that compress and cool off.
3. method as claimed in claim 2, wherein:
The fluid of discarding fluid and nitrogen product fluid and compression and purifying is in the heat exchange of main heat exchanger indirect;
Warm and the acting of expanding subsequently of discarded fluid part in main heat exchanger is discharged fluid to produce; And
Discharge fluid and introduce main heat exchanger and fully warm again with the refrigeration low-temperature distillation process.
4. the method for claim 1, wherein the pressure of oxygen enriched liquid fluid was adjusted before entering rectifying column.
5. method as claimed in claim 4, wherein the pressure of nitrogen-rich liquid fluid is adjusted by mechanical pumping nitrogen-rich liquid fluid.
6. method as claimed in claim 4, wherein the pressure of nitrogen-rich liquid fluid expands by the nitrogen-rich liquid Fluid valve and adjusts.
7. the method for claim 1, wherein:
The first of vapor phase fluid cools off in second heat exchanger fully to form the nitrogen-rich liquid fluid; And
The second portion of gaseous fluid is got back to rectifying column by warm, compression and cooling and recirculation.
8. method as claimed in claim 7, wherein:
The first oxygen enriched liquid fluid is by with nitrogen product fluid and discarded fluid indirect heat exchange and cold excessively; And
Compression and the fluid that purified combine to form fluid combination, that compress and purified with the second portion of vapor phase fluid after compression, and before compression, in conjunction with compression and the fluid that purified with nitrogen product fluid and the discarded fluid after crossing cold first oxygen enriched liquid fluid and nitrogen rich vapor fluid second portion, carry out indirect heat exchange and cool off, thereby form fluid that purified, compression and cooling by the compression of combination and the fluid that purified;
Wherein the second portion of vapor phase fluid is got back to rectifying column by combining to be cooled and to recycle with the fluid that compresses and purified.
9. method as claimed in claim 8, wherein:
The second portion of discarded fluid, nitrogen product fluid and vapor phase fluid and compression and the fluid that purified are in the heat exchange of main heat exchanger indirect;
Warm and the acting of expanding subsequently of discarded fluid part in main heat exchanger is discharged fluid to generate; And
Discharge fluid and introduce main heat exchanger and fully warm again with the refrigeration low-temperature distillation process.
10. a separation comprises the device of the admixture of gas of nitrogen and oxygen with the generation nitrogen product, and described device comprises:
Be connected in the rectifying column of main heat exchanger, by fluid purification, that compress and cool off that admixture of gas constitutes, generate cat head nitrogen rich vapor and oxygen enriched liquid tower bottom distillate with rectifying;
Be used to reduce pressure and comprise first valve to the first oxygen enriched liquid fluid of small part oxygen enriched liquid tower bottom distillate;
Be connected in first heat exchanger of first valve, to evaporate the first oxygen enriched liquid fluid;
Be connected in the phase separator of first heat exchanger, to separate gas phase the liquid phase that forms from the evaporation of the first oxygen enriched liquid fluid section;
Be connected in second valve of phase separator, being used to reduce pressure comprises the second oxygen enriched liquid fluid of Partial Liquid Phase at least;
Be connected in second heat exchanger of second valve and phase separator, with by with by vapor phase to small part vapor phase flow body indirect heat exchange with the part evaporate the second oxygen enriched liquid fluid, thereby fully be condensed to small part vapor phase fluid and form the nitrogen-rich liquid fluid;
Be connected in the 3rd heat exchanger of second heat exchanger, with the further evaporation second oxygen enriched liquid fluid;
Be connected in the rectifying column of first heat exchanger and the 3rd heat exchanger, with condensation by the cat head nitrogen rich vapor constitute to small part cat head nitrogen-rich stream and after condensation near small part cat head nitrogen-rich stream be back to rectifying column as backflow;
Be connected in second heat exchanger of rectifying column, introduce rectifying column with near small part nitrogen-rich liquid fluid above the fluid that purified, compress and cool off; And
Extraction comprises the equipment of the product nitrogen fluid of part cat head nitrogen rich vapor.
11. device as claimed in claim 10 further comprises:
Main heat exchanger, compression that constitutes by admixture of gas with cooling and the fluid that purified, and be formed up to fluid that small part purified, that compress and cool off;
Be connected in the subcooler of rectifying column, the discarded fluid indirect heat exchange that the oxygen enriched liquid fluid of winning is constituted by the vapor fraction after further evaporating with the nitrogen product fluid with by the second oxygen enriched liquid fluid, thus cold excessively; And
Also be connected in the main heat exchanger of subcooler, and be designed so that the fluid that compresses and purified is by cooling off with nitrogen product fluid and the discarded fluid indirect heat exchange after crossing cold first oxygen-rich fluid.
12. device as claimed in claim 11, wherein:
Main heat exchanger is designed so that discarded fluid and nitrogen product fluid and compression and the fluid indirect heat exchange that purified, and it is warm and the discharge fluid is complete warm to cool off this device in main switch to discard fluid part in main heat exchanger; And
Decompressor is connected in main heat exchanger, makes the warm discarded fluid afterwards of part expand acting to generate the discharge fluid in decompressor.
13. device as claimed in claim 10, wherein pump is between second heat exchanger and rectifying column, with pressurization nitrogen-rich liquid fluid after abundant condensation and before entering rectifying column.
14. device as claimed in claim 10, wherein the 3rd valve is between second heat exchanger and rectifying column, to reduce the pressure of nitrogen-rich liquid fluid before entering rectifying column.
15. device as claimed in claim 11, wherein:
Second heat exchanger is connected in phase separator, makes the fully condensation in second heat exchanger of the first of vapor phase fluid, to form the nitrogen-rich liquid fluid;
Compressor links to each other with the phase separator fluid and links to each other with main heat exchanger, and the second portion that main heat exchanger also is designed such that the vapor phase fluid is warm and compress in compressor in main heat exchanger; And
Main heat exchanger links to each other with the fluid and the compressor streaming flow that compress and purified simultaneously, make second portion and the compression of vapor phase fluid and the fluid that purified combine with compression that forms combination and the fluid that purified, in conjunction with compression and the fluid that purified in main heat exchanger, cool off with the fluid formation purification, that compress and cool off.
16. device as claimed in claim 15, wherein main heat exchanger also be designed so that the compression of combination and the fluid that purified by crossing discarded fluid after cold with nitrogen product fluid, first oxygen-rich fluid and the second portion indirect heat exchange of vapor phase fluid cools off.
17. device as claimed in claim 16, wherein:
Main heat exchanger is designed such that discarded fluid and nitrogen product fluid and compression and the fluid indirect heat exchange that purified, and it is warm and the discharge fluid is abundant warm to cool off this device in main heat exchanger to discard fluid part in main heat exchanger; And
Decompressor is connected in main heat exchanger makes the warm discarded fluid afterwards of part expand acting to generate the discharge fluid in decompressor.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US11/716493 | 2007-03-09 | ||
| US11/716,493 US20080216511A1 (en) | 2007-03-09 | 2007-03-09 | Nitrogen production method and apparatus |
| US11/716,493 | 2007-03-09 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN101285640A true CN101285640A (en) | 2008-10-15 |
| CN101285640B CN101285640B (en) | 2012-07-11 |
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Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN200810109272XA Expired - Fee Related CN101285640B (en) | 2007-03-09 | 2008-03-07 | Nitrogen production method and apparatus |
Country Status (6)
| Country | Link |
|---|---|
| US (1) | US20080216511A1 (en) |
| EP (1) | EP2126501B1 (en) |
| CN (1) | CN101285640B (en) |
| AT (1) | ATE488739T1 (en) |
| DE (1) | DE602008003541D1 (en) |
| WO (1) | WO2008112556A2 (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107031851A (en) * | 2015-09-25 | 2017-08-11 | 波音公司 | Nitrogen is generated and oxygen distribution system and the method for distribution oxygen-enriched air |
Families Citing this family (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US20100003184A1 (en) * | 2008-02-22 | 2010-01-07 | Toyota Jidosha Kabushiki Kaisha | Method for storing solar thermal energy |
| US8272216B2 (en) * | 2008-02-22 | 2012-09-25 | Toyota Jidosha Kabushiki Kaisha | Method for converting solar thermal energy |
| JP5365037B2 (en) | 2008-03-18 | 2013-12-11 | トヨタ自動車株式会社 | Hydrogen generator, ammonia burning internal combustion engine, and fuel cell |
| US8004102B2 (en) * | 2009-04-03 | 2011-08-23 | Praxair Technology, Inc. | Refrigeration generation method and system |
| DE102009038458A1 (en) * | 2009-08-21 | 2011-02-24 | Linde Ag | Process for separating nitrogen from natural gas |
| CN112556314A (en) * | 2020-12-31 | 2021-03-26 | 杭州制氧机集团股份有限公司 | Low-energy-consumption device for preparing pure nitrogen by using single tower and manufacturing method thereof |
Family Cites Families (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US3967464A (en) * | 1974-07-22 | 1976-07-06 | Air Products And Chemicals, Inc. | Air separation process and system utilizing pressure-swing driers |
| US4883519A (en) * | 1988-10-06 | 1989-11-28 | Air Products And Chemicals, Inc. | Process for the production of high pressure nitrogen with split reboil-condensing duty |
| US4867773A (en) * | 1988-10-06 | 1989-09-19 | Air Products And Chemicals, Inc. | Cryogenic process for nitrogen production with oxygen-enriched recycle |
| US4927441A (en) * | 1989-10-27 | 1990-05-22 | Air Products And Chemicals, Inc. | High pressure nitrogen production cryogenic process |
| JP3282040B2 (en) * | 1992-01-24 | 2002-05-13 | 日本酸素株式会社 | Ultra high purity oxygen sampling method and apparatus |
| US5551258A (en) * | 1994-12-15 | 1996-09-03 | The Boc Group Plc | Air separation |
| US5711167A (en) * | 1995-03-02 | 1998-01-27 | Air Liquide Process & Construction | High efficiency nitrogen generator |
| US5868006A (en) * | 1997-10-31 | 1999-02-09 | The Boc Group, Inc. | Air separation method and apparatus for producing nitrogen |
| US5934106A (en) * | 1998-01-27 | 1999-08-10 | The Boc Group, Inc. | Apparatus and method for producing nitrogen |
| US5899093A (en) * | 1998-05-22 | 1999-05-04 | Air Liquide Process And Construction, Inc. | Process and apparatus for the production of nitrogen by cryogenic distillation |
| JP4150107B2 (en) * | 1998-06-23 | 2008-09-17 | 大陽日酸株式会社 | Nitrogen production method and apparatus |
| US20010029749A1 (en) * | 2000-03-02 | 2001-10-18 | Robert Anthony Mostello | Method and apparatus for producing nitrogen from air by cryogenic distillation |
| US6330812B2 (en) * | 2000-03-02 | 2001-12-18 | Robert Anthony Mostello | Method and apparatus for producing nitrogen from air by cryogenic distillation |
-
2007
- 2007-03-09 US US11/716,493 patent/US20080216511A1/en not_active Abandoned
-
2008
- 2008-03-07 WO PCT/US2008/056239 patent/WO2008112556A2/en active Application Filing
- 2008-03-07 DE DE602008003541T patent/DE602008003541D1/en active Active
- 2008-03-07 AT AT08731689T patent/ATE488739T1/en not_active IP Right Cessation
- 2008-03-07 CN CN200810109272XA patent/CN101285640B/en not_active Expired - Fee Related
- 2008-03-07 EP EP08731689A patent/EP2126501B1/en not_active Not-in-force
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN107031851A (en) * | 2015-09-25 | 2017-08-11 | 波音公司 | Nitrogen is generated and oxygen distribution system and the method for distribution oxygen-enriched air |
Also Published As
| Publication number | Publication date |
|---|---|
| EP2126501A2 (en) | 2009-12-02 |
| WO2008112556A3 (en) | 2008-12-24 |
| CN101285640B (en) | 2012-07-11 |
| WO2008112556A2 (en) | 2008-09-18 |
| US20080216511A1 (en) | 2008-09-11 |
| DE602008003541D1 (en) | 2010-12-30 |
| EP2126501B1 (en) | 2010-11-17 |
| ATE488739T1 (en) | 2010-12-15 |
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