CN1760612A - Process for the cryogenic distillation of air - Google Patents
Process for the cryogenic distillation of air Download PDFInfo
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- CN1760612A CN1760612A CNA200510113618XA CN200510113618A CN1760612A CN 1760612 A CN1760612 A CN 1760612A CN A200510113618X A CNA200510113618X A CN A200510113618XA CN 200510113618 A CN200510113618 A CN 200510113618A CN 1760612 A CN1760612 A CN 1760612A
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- 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
- F25J3/04084—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 nitrogen
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- 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
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- 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
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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
- F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04436—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system
- F25J3/04442—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using at least a triple pressure main column system in a double column flowsheet with a high pressure pre-rectifier
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/30—Processes or apparatus using other separation and/or other processing means using a washing, e.g. "scrubbing" or bubble column for purification purposes
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- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
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- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
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Abstract
Pressurized gaseous nitrogen (''GAN'') is produced in a process in which liquid nitrogen (''LIN'') is produced in a cryogenic air separation unit (''ASU''). The pressure of at least a portion of the LIN is increased to produce pressurized LIN. A fluid having an oxygen concentration at least equal to that of air is separated in an auxiliary cryogenic distillation column to produce nitrogen-rich overhead vapor and oxygen-enriched bottoms liquid. Heat and optionally mass is transferred between at least a portion of the nitrogen-rich overhead vapor and at least a portion of the pressurized LIN to produce nitrogen-rich liquid and pressurized GAN. At least a portion of said nitrogen-rich liquid is used as reflux to the ASU after suitable pressure adjustment. Such a process allows the production of high purity GAN without the loss of oxygen recovery typically observed in conventional pumped LIN cycles.
Description
The present invention relates to a kind of cryogenic distillation method of air, the production of particularly high-purity, pressurized gaseous nitrogen (" GAN ").
High-purity GAN is usually in the cryogenic distillation of air process of preparing of carrying out pumping formula liquid nitrogen (" LIN ") circulation.In this circulation, the LIN pumping (pump) that will take from Distallation systm is to required product pressure, and in main heat exchanger by with condensation in the pressure-air indirect heat exchange evaporate.(" LAIR ") infeeds Tower System with the gained liquia air.Yet, when comparing with high pressure (" HP ") GAN circulation, adopt this pumping formula LIN circulation to cause disadvantageous oxygen to reclaim loss usually, in the high pressure GAN circulation nitrogen is taken out with the HP tower of steam form from the double tower distil system, in main heat exchanger, heat and be compressed to desired pressure.This be because: in pumping formula LIN circulation, will accompany by the nitrogen boiling and part material air pre-separation in the HP tower of condensation becomes in LIN and the thick liquid oxygen and not as the steam air raw material in the HPGAN circulation efficient equally.Thereby the lower pressure column of double tower system (" LP ") must more separate, and the overall oxygen of result reclaims and descends.
US-A-5419137 (Sweeney etc., May 30 nineteen ninety-five is open) has disclosed a kind of air separating method, produces high purity nitrogen with the double tower distil system.With condenser with the cat head in the LP tower (overhead) steam by partial condensation with high-purity LIN indirect heat exchange of taking from the HP tower.High-purity GAN shifts out as product with gained, but this product is a low pressure, and therefore needs nitrogen compressor separately and exclusively is to be compressed to the GAN product pressure of expectation.Condenser is positioned at the cat head part of LP tower.This piece list of references has also disclosed a kind of arrangement mode, wherein uses stripper (being often referred to as the overhead guard tower) the replacement condenser that is direct heat transfer and mass transfer relation with the LP tower.
US-A-4433989 (Erickson, on February 28th, 1984 is open) has disclosed a kind of air separating method, adopts the double tower system of being furnished with auxiliary destilling tower to produce GAN.In stand-by still, will be separated into liquid at the bottom of the overhead vapours of rich nitrogen and the tower of oxygen of concentrating from the thick liquid oxygen of HP tower storage tank.To reduce pressure and be used as the backflow of stand-by still from the LIN of HP tower.From this tower the cat head nitrogen rich vapor is taken out as product, do not extract the LIN product.
US-A-4433989 has also disclosed a kind of further stand-by still, wherein, and with the overhead vapours of air liquid and rich nitrogen at the bottom of this further is separated into the tower of oxygen enrichment in the stand-by still.This further stand-by still reflux with the cat head nitrogen steam by the indirect heat exchange condensation, this indirect heat exchange is and takes from the LP tower and undertaken by the pressurization LOX that pumping LOX provides.Further shift out the overhead vapours of condensation and infeed the HP tower the stand-by still from this as backflow.
US-A-6276171 (Brugerolle, August 21 calendar year 2001 open) has disclosed a kind of integrated gas turbine of air gas separation unit (" ASU ").LIN makes in ASU, and pumping also infeeds the nitrogen washing tower.GAN is shifted out, heats, compresses and mix with burnt gas from gas turbine before implementing to expand from the nitrogen washing tower with the pressure of 8-25bar (0.8-2.5MPa).Liquid shifts out, expands and infeed ASU from scrubbing tower at the bottom of the tower.Main hope is used to produce lower purified nitrogen with scrubbing tower.
US-A-5596886 (Howard, on January 28th, 1997 is open) has disclosed a kind of air separating method, produces gaseous oxygen (" GOX ") and high purity nitrogen with the double tower system of the stand-by still of being furnished with the nitrogen that concentrates.To heat, compress, cool off from the rich nitrogen overhead vapours of HP tower, infeed the stand-by still that refluxes with LIN then.The overhead vapours of the nitrogen that concentrates is shifted out from stand-by still, by with from the LOX indirect heat exchange of LP tower and condensation forms LIN.With the LIN pumping, and the LIN of part pumping infeeded the stand-by still top.
US-A-4790866 (Rathbone, on December 13rd, 1988 is open) has disclosed a kind of air separating method, adopts the double tower system of being furnished with argon column.LIN is shifted out and infeed the condenser of argon column from the HP tower after decompression, promote the condensation of argon column overhead vapours at this.
Need a kind of method, this method can be produced high-purity GAN and do not reduced the oxygen yield under the pressure that is different from this ASU operating pressure.
According to a first aspect of the invention, provide the method for a kind of pressurized gaseous nitrogen of production (" GAN "), this method comprises:
In cryogenic air separation unit (" ASU "), produce liquid nitrogen (" LIN ");
The described LIN pressurization of near small part is to produce the LIN of pressurization;
Identical with the air at least fluid of oxygen separation concentration in the assisted cryogenic destilling tower is with liquid at the bottom of the tower of the overhead vapours of producing rich nitrogen and the oxygen that concentrates;
At described rich nitrogen overhead vapours and the mass transfer that conducts heat and choose between the described pressurization LIN to small part, with the liquid of producing rich nitrogen and the GAN that pressurizes to small part; And
After suitable pressure was regulated, the liquid of the described rich nitrogen of near small part was supplied with ASU as refluxing.
Wording " rich nitrogen " is meant that nitrogen content is than high in the air.Wording " nitrogen that concentrates " is meant that nitrogen content is higher after having carried out the particular procedure step.Wording " oxygen enrichment " and " oxygen that concentrates " have similar implication with " the rich nitrogen " and " nitrogen that concentrates " that as above provides.The purity of the nitrogen-rich liquid purity than LIN usually is low, and the 85mol% nitrogen of preferably having an appointment is to the purity between about 99mol% nitrogen, for example about 95mol% nitrogen.
Preferable methods of the present invention makes it possible under different pressures production high-purity GAN from tower, usually anaerobic reclaims loss ground separating high-purity LIN in described tower, this oxygen reclaim loss usually in traditional pumping formula LIN circulation as seen, nitrogen seethes with excitement in this circulation, accompanies by air setting.
The required separation progression of preferable methods also still less.For example, in the embodiment of rich nitrogen overhead vapours condensation,, therefore only need less separation level because stand-by still need not to make pure LIN by making the LIN evaporation with the LIN indirect heat exchange.Between LIN and rich nitrogen overhead vapours, conduct heat and the embodiment of mass transfer in, the reflux ratio operation of the top of stand-by still when being higher than the logistics of not returning ASU, thereby the less separation level of needs just can reach identical purity level.
Compare with the circulation that high purity nitrogen directly seethes with excitement in scrubbing tower, this scrubbing tower does not have lower purified nitrogen to return ASU, and preferable methods is also more insensitive to operation exception.For example, rich nitrogen overhead vapours by with evaporation in the LIN indirect heat exchange and in the embodiment of condensation, stand-by still need not to make pure LIN and therefore only needs keep purity in the ASU tower of producing LIN.Between LIN and rich nitrogen overhead vapours, conduct heat and the embodiment of mass transfer in, the reflux ratio operation of top when being higher than the logistics of not returning ASU, thereby purity changes more insensitive to the operation in the reflux ratio.
In preferred embodiments, the opereating specification that can also enlarge nitrogen production (promptly can be efficiently, for example needn't discharge excessive nitrogen or infeed excess air ground, the scope of the nitrogen productivity ratio that provides to stand-by still), and in the situation of tower performance degradation, can more easily keep nitrogen purity.
After suitable pressure is regulated, with nitrogen-rich liquid as the backflow among the ASU.Comprise double tower distil system part at ASU, usually nitrogen-rich liquid is used as the backflow in the LP tower.Preferably, suitable pressure regulate or decompression after, the concentrate liquid of oxygen of also near small part infeeds ASU, may be as backflow.Comprise double tower distil system part at ASU, common near small part oxygen enriched liquid directly infeeds LP tower (although it can be infeeded through the HP tower, to be recovered in any steam that flashes off under the HP pressure tower).
The oxygen concentration of fluid is identical with air at least.Fluid can be for air or from the oxygen-rich fluid of ASU.Fluid can be gaseous state or liquid state.At fluid is in the method embodiment of liquid state, uses the near small part liquid of reboiler/condensor that is arranged in the stand-by still storage tank by evaporating with the process stream indirect heat exchange that suits subsequently usually.Suitable process stream for example comprises the effluent from LP or HP tower; If perhaps exist, from the effluent of argon column; Or the pressure-air supplied of booster air compressor effluent; The air stream or the nitrogen stream from the king-tower system of the nitrogen stream of recirculation or compression at low temperatures.
The pressure of LIN can be increased by hydrostatic head.Yet, preferably with the LIN pumping to increase its pressure.
Rich nitrogen overhead vapours can by with the LIN of pressurization indirectly or direct heat transfer and condensation.
Heat can to small part described rich nitrogen overhead vapours and to small part indirect exchange between the described pressurization LIN, thus, described rich nitrogen overhead vapours condensation is generated nitrogen-rich liquid and described pressurization LIN evaporation is generated the GAN that pressurizes.In this method embodiment, available reboiler/condensor indirect exchange heat.If reboiler/condensor is positioned on main distillation zone of stand-by still or the section, the LIN that pressurizes so just can pass reboiler/condensor, thus with the rich nitrogen overhead vapours condensation around the reboiler/condensor.If reboiler/condensor is positioned at the stand-by still skin, so rich nitrogen overhead vapours just can be passed reboiler/condensor, with the evaporation of the pressurization LIN around the reboiler/condensor.
Stand-by still comprises at least one main distillation zone usually.Can to small part described rich nitrogen overhead vapours and to small part direct heat transfer and mass transfer between the described pressurization LIN, generate nitrogen-rich liquid and pressurization GAN.In this embodiment, the gas/liquid contact promotion member that stand-by still preferably has at least one main distillation zone and is positioned at this top, main distillation zone.This method comprises makes rich nitrogen overhead vapours and pressurization LIN directly contact in contacting the promotion member, generates nitrogen-rich liquid and pressurization GAN.Contact promotes member normally another distillation zone (a further distillation zone).In this another distillation zone, liquid-gas ratio is much higher than from the not purity nitrogen steam at top, main distillation zone produces the required minimum of a value of high purity nitrogen.As a result, compare, can adopt less relatively distillation level with the method that does not have impure liquid nitrogen to return.
Stand-by still can reflux with any appropriate liquid, for example LAIR.Yet, preferably the part nitrogen-rich liquid is used to pass back into stand-by still.
ASU can comprise any suitable destilling tower and arrange, and comprises the single distillation column of producing LIN.Yet in the preferable methods embodiment, ASU is a double tower system, and this system comprises HP destilling tower and LP destilling tower, and HP tower and LP tower are by ASU reboiler/condensor thermal.In this class embodiment, this method further comprises:
In the HP tower, air separation become liquid at the bottom of rich nitrogen overhead vapours of HP and the oxygen enrichment tower;
Fluid separation applications becomes rich nitrogen overhead vapours of LP and LOX at the bottom of the near small part oxygen enrichment tower in the LP tower;
In described ASU reboiler/condensor,, generate described LIN by cooling off also partial condensation at least with the rich nitrogen overhead vapours of the near small part HP of the indirect heat exchange of LOX; And
With the described LIN backflow of part HP tower.
After suitable pressure is regulated, liquid at the bottom of the part oxygen enrichment tower that generates in the HP tower can be used as segment fluid flow at least.Liquid can pressurize by hydrostatic head at the bottom of the oxygen enrichment tower, but preferably pumps up.
In this class methods embodiment, the operating pressure of stand-by still is usually above the operating pressure of LP tower, and preferably is higher than the operating pressure of HP tower.Thus, the typical operation pressure of LP tower is about 1.2 crust (0.12MPa)-Yue 4 crust (0.4MPa), and the HP tower is about 4 crust (0.4MPa)-Yue 12 crust (1.2MPa).Preferred operating pressure is about 4.8 crust (0.48MPa) to the HP tower, is 1.3 crust (0.13MPa) to the LP tower.The operating pressure of stand-by still can be about 1.0 crust (0.10MPa)-Yue 30 crust (3.0MPa), is generally about 1.5 crust (0.15MPa)-Yue 25 crust (2.5MPa).Preferably, the operating pressure of stand-by still is about 12 crust (1.2MPa).
Pressurization GAN produces under the operating pressure of stand-by still usually, and under the pressure of about 1.0 crust (0.1MPa)-Yue 25 crust (2.5MPa), produce usually, and be generally high-purity, for example about 99.9mol% nitrogen-Yue 99.9999mol% nitrogen, typically about 99.99mol% nitrogen.
According to a second aspect of the invention, provide the device of producing pressurization GAN, this device comprises:
Comprise the low temperature ASU of at least one destilling tower, be used to produce LIN;
Pressing element is used for LIN is pressurizeed;
Pipe fitting is used for the LIN from the ASU cat head of producing described LIN is supplied with pressing element;
The assisted cryogenic destilling tower that comprises main distillation zone, be used for that the fluid that oxygen content is identical with air at least is separated into rich nitrogen overhead vapours and the tower of oxygen of concentrating at the bottom of liquid;
Can make and transmit the member carry out, be used for can to small part described rich nitrogen overhead vapours with conduct heat between the described pressurization LIN to small part and mass transfer randomly, to produce nitrogen-rich liquid and the GAN that pressurizes;
Pipe fitting, the pressurization LIN that is used for the member of self-pressurization are in the future supplied with to make and are transmitted the member that carries out;
Pressure relief mechanism is used to reduce the pressure of nitrogen-rich liquid to produce the nitrogen-rich liquid of decompression;
Pipe fitting is used for the nitrogen-rich liquid from stand-by still is supplied with pressure relief mechanism; And
Pipe fitting is used for the decompression nitrogen-rich liquid from described pressure relief mechanism is supplied with ASU as refluxing.
Can make and transmit the member that carries out can be the condensation member, is used for making to the condensation of the rich nitrogen overhead vapours of small part by the LIN indirect heat exchange with pressurization, generates nitrogen-rich liquid and pressurization GAN.In another embodiment, can make and transmit the member that carries out can be that the gas/liquid contact promotes member, for example another distillation zone is used to promote rich nitrogen overhead vapours and direct contact of pressurizeing between the LIN, and this contact promotes member to be positioned at top, the main distillation zone of auxiliary destilling tower.
As mentioned above, ASU can comprise single distillation column.But in preferred embodiments, ASU comprises two distillation column systems.In this embodiment preferred, can be with nitrogen-rich liquid or the supply HP tower or the supply LP tower of decompression.Also preferably the decompression before with its cold excessively (subcool) so that the formation of flash distillation minimize.
This device preferably also comprises: pressure relief mechanism is used to reduce and concentrates the pressure of oxygen liquid to produce the decompression oxygen liquid that concentrates; Pipe fitting is used for the oxygen liquid that concentrates from stand-by still is supplied with this pressure relief mechanism; And pipe fitting, be used for the oxygen liquid that concentrates from the decompression of this pressure relief mechanism is supplied with ASU, can be used as backflow.If ASU comprises double tower system, the oxygen liquid that concentrates that will reduce pressure is so usually supplied with the LP tower, passes through the bottom of HP tower usually.
Every kind of pressure relief mechanism can be any suitable member that is used to reduce cryogenic liquid or gas pressure.Yet preferred pressure relief mechanism is an expansion valve, for example the Joule-Thompson valve.
Can adjust and/or construct this device, make it possible to implement any above-mentioned preferable methods embodiment.
The particularly preferred embodiment of this method or device is fully described as mentioned, in conjunction with the accompanying drawings.
Now will the preferred embodiments of the invention be described in conjunction with the accompanying drawings, wherein:
Fig. 1 is the diagram that is applicable to a kind of stand-by still of the present invention;
Fig. 2 is the diagram that is applicable to another kind of stand-by still of the present invention;
Fig. 3 is the flow chart according to a kind of embodiment of the inventive method;
Fig. 4 is the flow chart according to the another embodiment of the inventive method;
Fig. 5 is the flow chart according to another embodiment of the inventive method; And
Fig. 6 is by the flow chart of method for computer simulation among the embodiment.
With reference to Fig. 1, with air or oxygen-rich fluid (if for example with pump (not shown) or raw material be steam with after the pressurization of compressor (not shown) from liquid at the bottom of the oxygen enrichment tower of HP tower in the double tower ASU (not shown),) logistics 12 supply with the bottom of auxiliary destilling tower 14, liquid at the bottom of this is separated into it in tower of the overhead vapours of rich nitrogen and the oxygen that concentrates.When fluid is liquid, use optional reboiler/condensor 16 by small part fluid evaporator near with the indirect heat exchange of process stream.
Take out pure LIN logistics 18 and pumping pump 20 from ASU.The reboiler/condensor 24 that is positioned at stand-by still 14 outsides is supplied with in the logistics 22 of pressurization LIN, by evaporating, generated the logistics 26 of pressurization GAN and as the nitrogen-rich liquid of the backflow of stand-by still 14 with indirect heat exchange from the rich nitrogen overhead vapours of stand-by still 14 at this.Take out nitrogen-rich liquid logistics 28 from stand-by still 14, after suitable pressure is regulated, supply with the ASU (not shown) as refluxing.From the logistics 30 that stand-by still 14 takes out the oxygen bottom body that concentrates, after suitable pressure is regulated, supply with the ASU (not shown) as refluxing equally.
Similar to shown in Fig. 1 of process shown in Fig. 2, identical Reference numeral is used in reference to and is shown in feature identical among each figure.Below describe and only relate to the feature different shown in Figure 2 with feature shown in Fig. 1.
Among Fig. 2, reboiler/condensor 24 replaces with distillation zone other in the stand-by still 14 or section 32.Rich nitrogen overhead vapours directly contacts with pressurization LIN from logistics 22 in this other destilling tower section 32.Conduct heat simultaneously and mass transfer, generate nitrogen-rich liquid (shifting out) and pressurization GAN (shifting out) as logistics 26 as logistics 28.
Referring now to Fig. 3, the logistics 100 of raw air is compressed in compressor 102, with clean unit 104 water and carbon dioxide is shifted out from gained compression raw air stream.The compression raw air that purifies is divided into three bursts of logistics 106,108 and 122.
The logistics 106 of compression raw air is further compression in compressor 115, with this further raw air of compression in main heat exchanger 112, be cooled to medium temperature between its Wen Duanyu cold junction, shift out as logistics 116 thus and expansion in expander 118, for this process provides refrigeration.To deliver to the centre position of two distillation column system LP towers 150 through the raw air logistics 120 that expands.
To be separated into liquid and the rich nitrogen overhead vapours of HP tower at the bottom of the HP tower oxygen enrichment tower as the raw airs that HP towers 124 are supplied with in logistics 110 and 128.To be separated into liquid and the rich nitrogen overhead vapours of stand-by still at the bottom of the stand-by still oxygen enrichment tower as the raw air that stand-by stills 196 are supplied with in logistics 127.The logistics 167 of liquid at the bottom of the stand-by still oxygen enrichment tower is shifted out from stand-by still 196,, form liquid stream 152 at the bottom of the oxygen enrichment tower with combining, this logistics 152 is delivered to the centre position of LP tower 150 through valve 153 from liquid at the bottom of the HP tower oxygen enrichment tower of HP tower through valve 168 decompression.Liquid stream 130 shifts out from the centre position of HP tower 124, and is supplying with LP tower 150 after valve 131 decompressions.
The logistics 158 of the rich nitrogen overhead vapours of the HP tower cat head from HP tower 124 is shifted out, by condensation, generate LIN logistics 162 with the LOX indirect heat exchange at the condenser 160 that is arranged in LP tower 150 storage tanks.A part is delivered to the top of HP tower 124 as backflow from the LIN of logistics 162.Second portion is delivered to the top of LP tower 150 as backflow after reducing pressure through valve 171 with logistics 170.Third part generates pressurization LIN logistics 165 at this with its pumping with logistics 163 supply pumps 164.
The logistics 165 of pressurized stream LIN is seethed with excitement by logistics 159 indirect heat exchanges with the rich nitrogen overhead vapours of stand-by still in reboiler/condensor 161, generates pressurization GAN logistics 166 and nitrogen-rich liquid logistics.Pressurization GAN logistics 166 is heated in main heat exchanger 112, accompanies by the raw air cooling, generates pressurization GAN product stream 168.The part nitrogen-rich liquid is delivered to the top of stand-by still 196 as backflow, and remainder is delivered to the top of LP tower 150 with logistics 169 as backflow after reducing pressure through valve 173.
The feed stream of LP tower 150 is separated into LP cat head nitrogen steam and LOX.LOX logistics 180 shifts out from LP tower 150, and pressurization in pump 182 generates the logistics 184 of pressurization LOX, and this logistics 184 is heated in main heat exchanger 112 generates GOX logistics 186.The logistics 172 of gaseous nitrogen shifts out from the cat head of LP tower 150, heats to generate LPGAN logistics 176 in main heat exchanger 112.
Similar to shown in Fig. 3 of process shown in Fig. 4-6, identical Reference numeral is used in reference to and is shown in feature identical among each figure.Below describe and only relate to features different shown in Fig. 4-6 with feature shown in Fig. 3.
Among Fig. 4, it is opposite that stand-by still 196 does not have reboiler/condensor 161., and this tower has the further distillation zone 503 that is positioned on the main distillation zone 501.The top of stand-by still 196 is delivered in the logistics 165 of pressurization LIN, and the logistics 166 of pressurization GAN is shifted out from the top of stand-by still 196.The logistics 169 of nitrogen-rich liquid is shifted out from the centre position in the stand-by still 196, and at the top of after valve 173 decompressions, delivering to LP tower 150.
Similar to shown in Fig. 4 of process shown in Fig. 5, stand-by still 196 has the further distilling period 503 that is positioned on the main distilling period 501.Intermediate reflux to HP tower 124 is provided by the nitrogen-rich liquid logistics 169 through valve 173 decompressions.Backflow to LP tower 150 is provided by logistics 170, and this logistics 170 extracts from the centre position of HP tower, through valve 171 decompressions, delivers to the top of LP tower 150 then.
Similar to shown in Fig. 3 of process shown in Fig. 6, stand-by still 196 has reboiler/condensor 161.Main difference is the air raw material of process.Among Fig. 6, air logistics 100 is compressed in compressor 102, and will compress logistics and purify in clarifier 104 to remove and anhydrate and carbon dioxide.With the compressed air stream 105 that purifies be divided into three stocks from logistics 107,108 and 122.
The compressed air stream 108 that purifies cool off in main heat exchanger 112 and the logistics of cooling off 110 is expanded in expander 118, for process provides the part refrigerating capacity.Gained expanded air stream is delivered to the bottom of HP tower 124.
From condenser 161 flow to LP tower 150 nitrogen-rich liquid logistics 169, from HP tower 124 flow to condenser 161 through the LIN of pumping logistics 165, flow to the LIN logistics 170 of LP tower 150 and all pass through to small part main heat exchanger 112 from the fluid stream 130 that HP tower 124 centre positions flow to the LIN of LP tower 150 from HP tower 124, thereby the temperature of regulating every kind of logistics with its tower that is infeeded in the temperature of position mate better.For the sake of simplicity, not shown logistics when flowing through main heat exchanger 112, but show heat exchanger 112 with decomposed form (as split up).
Different among process among Fig. 6 and Fig. 3 also are the LOX logistics 185 of LIN logistics 190 and pumping is drifted as product.
Embodiment
Carried out the computer simulation of process shown in Fig. 6, with illustration the present invention.In this simulation, stand-by still 196 has only 10 theoretical stages, yet will need about 50 grades if directly produce purity nitrogen with the remainder that does not make purity nitrogen not return ASU.Simulation result is shown in Table 1.
Table 1
| Feed stream | 105 | 107 | 108 | 122 | 325 | |
| F P T ％O 2 ％N 2The %Ar phase | Kmol/h bar (MPa) degree centigrade ℃ | 10,000 13.4 (1.34) 30 20.96 78.11 0.93 Zheng gas | 2,917 13.4 (1.34) 30 20.96 78.11 0.93 Zheng gas | 4,667 13.4 (1.34) 30 20.9 6 78.11 0.93 Zheng gas | 2,416 13.4 (1.34) 30 20.96 78.11 0.93 Zheng gas | 2,519 13.4 (1.34) 30 20.96 78.11 0.93 Zheng gas |
| Product stream | 168 | 176 | 185 | 186 | 190 | |
| F P T ％O 2 ％N 2The %Ar phase | Kmol/h bar (MPa) degree centigrade ℃ | 2,526 12.5 (1.25) 27 1ppm, 99.89 0.11 Zheng gas | 5,693 1.2 (0.12) 27 6.50 92.00 1.50 Zheng gas | 42 34 (3.4)-177.7 99.8 5 0.00 0.15 liquid | 1,688 33.4 (3.34) 27 99.85 0.00 0.15 Zheng gas | 51 4.9 (0.49)-189.3 1ppm, 99.89 0.11 liquid |
| Intermediate stream | 127 | 165 | 166 | 167 | 169 | |
| F P T ％O 2 ％N 2The %Ar phase | Kmol/h bar (MPa) degree centigrade ℃ | 2,519 12.8 (1.28)-161 20.96 78.11 0.93 Zheng gas | 2,526 12.7 (1.27)-170.3 1ppm, 99.89 0.11 liquid | 2,526 12.7 (1.27)-165.4 1ppm, 99.89 0.11 Zheng gas | 1,189 12.8 (1.28)-161 33.90 64.90 1.20 liquid | 1,330 2.7 (1.27)-164.3 9.40 90.00 0.60 liquid |
Run through specification in the whole text, about the term " member " in the content of the member of implementing certain function be intended to refer to through adjust and/or structure to implement at least a equipment of this function.
Be appreciated that to the invention is not restricted to the above details of describing with reference to preferred embodiment, but can carry out multiple change or distortion and do not depart from the spirit and scope of the invention that limits as following claim.
Claims (26)
1. method of producing pressurized gaseous nitrogen (" GAN "), this method comprises:
In cryogenic air separation unit (" ASU "), produce liquid nitrogen (" LIN ");
The pressure that increases to the described LIN of small part is to produce the LIN of pressurization;
Identical with the air at least fluid of oxygen separation concentration in the assisted cryogenic destilling tower is with liquid at the bottom of the tower of the overhead vapours that generates rich nitrogen and the oxygen that concentrates;
In described rich nitrogen overhead vapours and to conducting heat between the LIN of the described pressurization of small part and mass transfer randomly, with liquid and the pressurization GAN that generates rich nitrogen to small part; And
After suitable pressure was regulated, the liquid of the described rich nitrogen of near small part was supplied with ASU as refluxing.
2. the method described in claim 1, wherein after suitable pressure was regulated, the liquid of the described oxygen that concentrates of near small part was supplied with ASU.
3. the method described in claim 1, wherein said fluid is an air.
4. the method described in claim 1, wherein said fluid is the oxygen-rich fluid from ASU.
5. the method described in claim 1 wherein is used to pass back into described stand-by still with the described nitrogen-rich liquid of part.
6. the method described in claim 1, wherein with described partial L IN pumping to increase its pressure.
7. the method described in claim 1, wherein heat to small part described rich nitrogen overhead vapours and to small part indirect exchange between the described pressurization LIN, thus described rich nitrogen overhead vapours condensation is generated nitrogen-rich liquid, described pressurization LIN evaporation is generated pressurization GAN.
8. the method described in claim 7, wherein said heat reboiler/condensor indirect exchange.
9. the method described in claim 1, wherein to small part described rich nitrogen overhead vapours and to small part direct heat transfer and mass transfer between the described pressurization LIN, generate nitrogen-rich liquid and pressurization GAN.
10. the method described in claim 9, wherein the stand-by still gas/liquid contact that has at least one main distillation zone and be positioned at this top, main distillation zone promotes member, described method is included in described contact and promotes to make in the member rich nitrogen overhead vapours directly to contact with pressurization LIN, generates described nitrogen-rich liquid and pressurization GAN.
11. the method described in claim 10, wherein said contact promote that member is another distillation zone.
12. the method described in claim 1, wherein said fluid is a gaseous state.
13. the method described in claim 1, wherein said fluid is a liquid.
14. the method described in claim 13 is wherein evaporated by the described liquid of small part near with the indirect heat exchange of process stream with the reboiler/condensor that is positioned at described stand-by still storage tank.
15. the method described in claim 1, wherein ASU comprises higher pressure (" HP ") destilling tower and than low pressure (" LP ") destilling tower, and described HP tower and described LP tower are by the thermally coupled of ASU reboiler/condensor, and described method further comprises:
In described HP tower, air separation become liquid at the bottom of rich nitrogen overhead vapours of HP and the oxygen enrichment tower;
Fluid separation applications becomes rich nitrogen overhead vapours of LP and liquid oxygen (" LOX ") at the bottom of the described oxygen enrichment tower of near small part in described LP tower;
In described ASU reboiler/condensor,, generate described LIN by cooling off also partial condensation at least with the rich nitrogen overhead vapours of the described HP of the near small part of LOX indirect heat exchange; And
With the described LIN of the part described HP tower that refluxes.
16. the method described in claim 15, after further being included in suitable pressure and regulating, with liquid at the bottom of the described oxygen enrichment tower of part as to the described fluid of small part.
17. the method described in claim 15, the operating pressure of wherein said stand-by still is higher than the operating pressure of described LP tower.
18. the method described in claim 15, the operating pressure of wherein said stand-by still is higher than the operating pressure of described HP tower.
19. the method for claim 1, wherein the operating pressure of stand-by still is 0.1MPa (1.0 crust)-3.0MPa (30 crust).
20. the method described in claim 1, the GAN that wherein pressurizes produces under the pressure of 0.15MPa (1.5 crust)-2.5MPa (25 crust).
21. the method described in claim 1, the purity of wherein said pressurization GAN are 99.9mol% nitrogen-99.9999mol% nitrogen.
22. produce the device of pressurization GAN, this device comprises:
Comprise the low temperature ASU of at least one destilling tower, be used to produce LIN;
Pressing element is used for LIN is pressurizeed;
Pipe fitting is used for the LIN from the ASU cat head of producing described LIN is supplied with pressing element;
The assisted cryogenic destilling tower that comprises main distillation zone, be used for that the fluid that oxygen content is identical with air at least is separated into rich nitrogen overhead vapours and the tower of oxygen of concentrating at the bottom of liquid;
Can make and transmit the member carry out, be used for can to small part described rich nitrogen overhead vapours with conduct heat between the described pressurization LIN to small part and mass transfer randomly, to produce nitrogen-rich liquid and the GAN that pressurizes;
Pipe fitting, the pressurization LIN that is used for the member of self-pressurization are in the future supplied with to make and are transmitted the member that carries out;
Pressure relief mechanism is used to reduce the pressure of nitrogen-rich liquid to produce the nitrogen-rich liquid of decompression;
Pipe fitting is used for the nitrogen-rich liquid from stand-by still is supplied with pressure relief mechanism; And
Pipe fitting is used for the decompression nitrogen-rich liquid from described pressure relief mechanism is supplied with ASU as refluxing.
23. the device described in claim 22, wherein can make and transmit the member that carries out is the condensation member, is used for making to the condensation of the rich nitrogen overhead vapours of small part by the indirect heat exchange with pressurization LIN, generates nitrogen-rich liquid and pressurization GAN.
24. the device described in claim 22, the wherein said member that transmission is carried out is that the gas/liquid contact promotes member, be used to promote rich nitrogen overhead vapours and direct contact of pressurizeing between the LIN, described contact promotes member to be positioned at top, the main distillation zone of auxiliary destilling tower.
25. the device described in claim 24, wherein contact promotes that member is another distillation zone in the stand-by still.
26. the device described in claim 22 further comprises:
Pressure relief mechanism is used to reduce and concentrates the pressure of oxygen liquid to produce the decompression oxygen liquid that concentrates;
Pipe fitting is used for the oxygen liquid that concentrates from stand-by still is supplied with this pressure relief mechanism; With
Pipe fitting is used for the oxygen liquid that concentrates from the decompression of this pressure relief mechanism is supplied with ASU.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| GBGB0422635.3A GB0422635D0 (en) | 2004-10-12 | 2004-10-12 | Process for the cryogenic distillation of air |
| GB0422635.3 | 2004-10-12 |
Publications (1)
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| CN1760612A true CN1760612A (en) | 2006-04-19 |
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| CNA200510113618XA Pending CN1760612A (en) | 2004-10-12 | 2005-10-12 | Process for the cryogenic distillation of air |
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| US (1) | US20060075779A1 (en) |
| EP (1) | EP1653183A1 (en) |
| CN (1) | CN1760612A (en) |
| GB (1) | GB0422635D0 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101925790A (en) * | 2008-01-28 | 2010-12-22 | 林德股份公司 | Method and device for low-temperature air separation |
| CN104006628A (en) * | 2013-02-21 | 2014-08-27 | 林德股份公司 | Method and device for obtaining high-pressure oxygen and high-pressure nitrogen |
| CN108168210A (en) * | 2018-01-25 | 2018-06-15 | 江西江氨科技有限公司 | Method for producing oxygen through and system |
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| US7437890B2 (en) * | 2006-01-12 | 2008-10-21 | Praxair Technology, Inc. | Cryogenic air separation system with multi-pressure air liquefaction |
| US7712331B2 (en) * | 2006-06-30 | 2010-05-11 | Air Products And Chemicals, Inc. | System to increase capacity of LNG-based liquefier in air separation process |
| US8136369B2 (en) * | 2006-07-14 | 2012-03-20 | L'air Liquide Societe Anonyme Pour L'etude | System and apparatus for providing low pressure and low purity oxygen |
| EP2227624B1 (en) * | 2007-12-06 | 2020-04-29 | Sustainable Energy Solutions, LLC | Methods and systems for generating power from a turbine using pressurized nitrogen |
| DE102009048456A1 (en) * | 2009-09-21 | 2011-03-31 | Linde Aktiengesellschaft | Method and apparatus for the cryogenic separation of air |
| EP2312247A1 (en) * | 2009-10-09 | 2011-04-20 | Linde AG | Method and device for generating liquid nitrogen from low temperature air separation |
| WO2020169257A1 (en) | 2019-02-22 | 2020-08-27 | Linde Gmbh | Method and system for low-temperature air separation |
| EP3771873A1 (en) * | 2019-08-01 | 2021-02-03 | Linde GmbH | Method and system for cryoseparation of air |
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| US4433989A (en) * | 1982-09-13 | 1984-02-28 | Erickson Donald C | Air separation with medium pressure enrichment |
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| US5098457A (en) * | 1991-01-22 | 1992-03-24 | Union Carbide Industrial Gases Technology Corporation | Method and apparatus for producing elevated pressure nitrogen |
| US5419137A (en) | 1993-08-16 | 1995-05-30 | The Boc Group, Inc. | Air separation process and apparatus for the production of high purity nitrogen |
| US5596886A (en) | 1996-04-05 | 1997-01-28 | Praxair Technology, Inc. | Cryogenic rectification system for producing gaseous oxygen and high purity nitrogen |
| DE19735154A1 (en) * | 1996-10-30 | 1998-05-07 | Linde Ag | Producing compressed nitrogen@ by low temperature distillation of air in rectifier system |
| GB9724787D0 (en) * | 1997-11-24 | 1998-01-21 | Boc Group Plc | Production of nitrogen |
| US6276171B1 (en) | 1999-04-05 | 2001-08-21 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Integrated apparatus for generating power and/or oxygen enriched fluid, process for the operation thereof |
| US6202442B1 (en) * | 1999-04-05 | 2001-03-20 | L'air Liquide, Societe Anonyme Pour L'etude Et L'expoitation Des Procedes Georges Claude | Integrated apparatus for generating power and/or oxygen enriched fluid and process for the operation thereof |
| FR2795496B1 (en) * | 1999-06-22 | 2001-08-03 | Air Liquide | APPARATUS AND METHOD FOR SEPARATING AIR BY CRYOGENIC DISTILLATION |
| DE19933558C5 (en) * | 1999-07-16 | 2010-04-15 | Linde Ag | Three-column process and apparatus for the cryogenic separation of air |
| US6397631B1 (en) * | 2001-06-12 | 2002-06-04 | Air Products And Chemicals, Inc. | Air separation process |
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| DE10339221A1 (en) * | 2003-08-26 | 2005-03-24 | Linde Ag | Production of pressurized nitrogen by low temperature decomposition of air in rectifier system comprises condensing no gas from upper region of high pressure column in indirect heat exchange with liquid from low pressure column |
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- 2004-10-12 GB GBGB0422635.3A patent/GB0422635D0/en not_active Ceased
-
2005
- 2005-10-06 EP EP05256250A patent/EP1653183A1/en not_active Withdrawn
- 2005-10-06 US US11/246,853 patent/US20060075779A1/en not_active Abandoned
- 2005-10-12 CN CNA200510113618XA patent/CN1760612A/en active Pending
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| Publication number | Priority date | Publication date | Assignee | Title |
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| CN101925790A (en) * | 2008-01-28 | 2010-12-22 | 林德股份公司 | Method and device for low-temperature air separation |
| CN101925790B (en) * | 2008-01-28 | 2015-10-21 | 林德股份公司 | For the method and apparatus of low temperature air separating |
| CN104006628A (en) * | 2013-02-21 | 2014-08-27 | 林德股份公司 | Method and device for obtaining high-pressure oxygen and high-pressure nitrogen |
| CN104006628B (en) * | 2013-02-21 | 2017-11-28 | 林德股份公司 | Method and apparatus for obtaining hyperbaric oxygen and elevated pressure nitrogen |
| CN108168210A (en) * | 2018-01-25 | 2018-06-15 | 江西江氨科技有限公司 | Method for producing oxygen through and system |
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| Publication number | Publication date |
|---|---|
| GB0422635D0 (en) | 2004-11-10 |
| US20060075779A1 (en) | 2006-04-13 |
| EP1653183A1 (en) | 2006-05-03 |
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