US20130340476A1 - Apparatus and method for separating air by cryogenic distillation - Google Patents
Apparatus and method for separating air by cryogenic distillation Download PDFInfo
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- US20130340476A1 US20130340476A1 US14/003,902 US201214003902A US2013340476A1 US 20130340476 A1 US20130340476 A1 US 20130340476A1 US 201214003902 A US201214003902 A US 201214003902A US 2013340476 A1 US2013340476 A1 US 2013340476A1
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- oxygen
- exchanger
- pressure
- sending
- purge
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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
- F25J3/0228—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 characterised by the separated product 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—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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- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
- F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
- F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
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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
- F25J3/04303—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
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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
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04418—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system with thermally overlapping high and low pressure columns
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04812—Different modes, i.e. "runs" of operation
- F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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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
- F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
- F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- 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
- F25J2250/40—One fluid being air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J2250/50—One fluid being 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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/62—Details of storing a fluid in a tank
Definitions
- This invention relates to an apparatus and method for separating air by air distillation.
- gaseous oxygen in particular, it relates to the production of gaseous oxygen at a pressure below 9 bars abs, even below 5 bars abs.
- the gaseous oxygen can possibly contain less than 98% mol. oxygen.
- this invention proposes to vaporise the deconcentration purge of a vaporiser in an exchanger in order to recover the refrigeration, this vaporiser being the exchanger making it possible to vaporise a liquid of the apparatus under pressure in order to produce a pressurised gaseous product.
- an apparatus for separating air comprising a double column comprising a medium-pressure column and a low-pressure column, a main exchanger, a vaporiser, a main compressor, means for sending all of the air to be treated in the double column to the main compressor in order to produce air substantially at the pressure P 1 of the medium-pressure column, means for sending a portion of the air substantially at a high pressure P 2 to the main exchanger and then to the vaporiser, a pipe for sending air at least partially condensed in the vaporiser to at least one of the columns, a pipe for sending air at the pressure P 1 to the medium-pressure column, means of pressurising, a pump, a pipe for withdrawing the liquid oxygen from the low-pressure column and for sending it to the means of pressurising, a pipe for sending liquid oxygen that has been pressurised at a pressure below 9 bar abs from the means of pressurising to the vaporiser, a pipe for sending gaseous oxygen from the vaporiser to the
- a method for separating air in an apparatus comprising a double column comprising a medium-pressure column and a low-pressure column, a main exchanger, a vaporiser, a main compressor, means of pressurising, a pump, wherein all the air to he treated is sent in the double column to the main compressor in order to produce air substantially at the pressure P 1 of the medium-pressure column, a portion of the air substantially at a high pressure P 2 is sent to the main exchanger and then to the vaporiser, air at least partially condensed in the vaporiser is sent to at least one of the columns, air at the pressure P 1 is sent to the medium-pressure column, liquid oxygen is withdrawn from the low-pressure column and it is pressurised, the liquid oxygen that has been pressurised is sent at a pressure below 5 bar abs to the vaporiser, a first flow of gaseous oxygen is sent from the vaporiser to the main exchanger to be heated and liquid purge oxygen of the vaporiser is pressurised
- FIG. 1 shows an embodiment of the present invention.
- FIG. 2 shows another embodiment of the present invention.
- the apparatus comprises an exchange line 21 and a double column constituted of a medium-pressure column 27 and a low-pressure column 29 .
- All of the air I is compressed in the main compressor 2 in order to produce air at the pressure P 1 substantially equal to the pressure of the medium-pressure column 27 .
- the air at the pressure P 1 is cooled in a cooler 7 , purified in a purification unit 9 and divided into three fractions.
- the first fraction 11 is supercharged in a supercharger, able to be constituted of the last stage of the main compressor, with this last stage being part of the second portion of the compressor.
- the pressure P 1 is below 5 bars abs, even 4.5 bar abs, preferably below 4 bar, and even below 3.5 bar abs.
- the first fraction 11 is brought to a pressure P 2 by the booster 5 or an independent compressor 5 and cooled at this pressure in a cooler (not shown) before being sent to the exchange line 21 .
- the exchange line is comprised of a brazed-plate aluminium indirect heat exchanger.
- the fraction 11 is then sent in gaseous form to a vaporiser 41 where it is condensed at least partially before being expanded and sent to the medium-pressure column 27 .
- the pressure P 2 is below 15 bar abs, preferably below 10 bar, and even below 6 bar abs.
- the fraction 11 . is less than half of the flow 1 , and preferably less than a third of the flow 1 .
- the second fraction 1.3 at the pressure P 1 is cooled entirely in the exchange line 21 and is divided into two flows.
- the first flow 23 is sent to a tank reboiler 33 from the low-pressure column 29 where it is condensed at least partially and is sent to the medium-pressure column, mixed with the flow 11 .
- the second flow 25 is sent in gaseous form to the median-pressure column 27 .
- the third fraction 15 is pressurized in a boostercharger 17 , partially cooled in the exchange line 21 , withdrawn from the exchange line at an intermediary level of the latter and expanded in a turbine 19 coupled to the supercharger 17 before being sent to the low-pressure column 29 .
- a flow of oxygen-rich liquid 55 , an intermediate flow 53 and a flow of nitrogen-rich liquid 51 are withdrawn from the medium-pressure column 27 , cooled in the exchanger 31 , expanded and sent to different levels of the low-pressure column 29 .
- Medium-pressure gaseous nitrogen 49 is condensed in an intermediate vaporiser 35 of the low-pressure column 29 and sent as a reflux at the head of the medium pressure column 27 . Another flow of medium-pressure gaseous nitrogen 47 is heated in the exchange line.
- Liquid oxygen 37 containing at least 80% mol. oxygen and possibly at most 98% mol. oxygen, is withdrawn from the tank of the low-pressure column 29 , pressurised by a pump 39 at a pressure below 9 bars abs, even below 5 bars abs and sent to the vaporiser 41 .
- the oxygen is vaporised in the vaporiser 41 by exchange of heat with the fraction of air 11 at the pressure P 2 .
- This oxygen then forms the first flow of pressurised gaseous oxygen 45 which is heated in the exchange line 21 .
- the fraction of air 11 is partially condensed and is sent to the double column.
- the purge liquid 43 is pressurised to a pressure of at least 10 bars abs, or at least 15 bar abs, even at least 20 bars abs in a pump 63 then is vaporised in the exchange line 21 .
- the second gaseous flow produced as such 59 is sent to a storage of pressurised gases 3 and expanded in order to be mixed with the flow 45 via the pipe 61 .
- the pressurised purge liquid 43 can be vaporised in an auxiliary exchanger 21 A, separate from the exchange line, against an airflow 25 A and with a liquid refrigerant, for example a flow of nitrogen 57 A heated with the method of separating.
- the flow 25 A cooled in the exchanger 21 A is mixed with the cooled flow 25 and the flow of nitrogen 57 A heated in the exchanger 21 A is mixed with the heated flow 57 .
- the second flow of gaseous oxygen 59 , 61 formed by the vaporisation can be used as a backup gas during an interruption of the production of gaseous oxygen 45 .
- the pressurisation by the pump 39 and/or 63 can be replaced with a hydrostatic pressurisation in all of the eases described.
- variable quantity of the second flow of gaseous oxygen is mixed with the first flow in order to produce a substantially constant mixed flow.
- This variable quantity of the vaporised purge liquid can be mixed with the first flow 45 in order to smooth. out the variations of flow, due, for example to variations of the pressure of the oxygen network.
- oxygen By detecting a reduction in pressure in the line 45 , due, for example to an increased oxygen demand, oxygen can be expanded and sent from storage 3 to the line 45 via the pipe 61 .
- the flow of oxygen 45 will be reduced or will be nonexistent.
- the flow of oxygen 63 from storage 3 can supply a client, the time for a backup vaporiser to be operational in order to prevent any stoppage of production.
- the flow 37 is the only flow containing more than 60% mol. oxygen withdrawn from the low-pressure column.
- the storage 3 operates at a pressure that is higher than the flow 45 .
- “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of” and “consisting of” unless otherwise indicated herein.
- Providing in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
- Optional or optionally means that the subsequently described event or circumstances may or may not occur.
- the description includes instances where the event or circumstance occurs and instances where it does not occur.
- Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Health & Medical Sciences (AREA)
- Emergency Medicine (AREA)
- Separation By Low-Temperature Treatments (AREA)
Abstract
Device for separating air comprises a pipe for withdrawing liquid oxygen from the low-pressure column and for sending it to a first pump, a pipe for sending liquid oxygen that has been pressurized to a pressure of below 9 bar as from the first pump to a vaporizer, a pipe for sending gaseous oxygen from the vaporizer to a main exchanger Where it is heated up, a pipe for sending liquid oxygen for purging from the vaporizer to a second pump to pressurize it and a pipe for sending the pressurized oxygen from the second pump to an exchanger where it vaporizes to form gaseous oxygen.
Description
- This application is a §371 of International PCT Application PCT/FR2012/050500, filed Mar. 9, 2012, which claims the benefit of FR 1152272, filed Mar. 18, 2011, both of which are herein incorporated by reference in their entireties.
- This invention relates to an apparatus and method for separating air by air distillation.
- In particular, it relates to the production of gaseous oxygen at a pressure below 9 bars abs, even below 5 bars abs. The gaseous oxygen can possibly contain less than 98% mol. oxygen.
- It is required to produce large quantities of oxygen having these characteristics in order to supply oxy-combustion apparatuses, among others.
- It is known in WO-A-10/109149 to vaporise a flow of liquid oxygen at low pressure in an exterior vaporiser in order to produce gaseous oxygen which is then heated in a main exchanger.
- It is known to vaporise the purge of a distillation column in order to recover its refrigeration, for example in U.S. Pat. No. 5,408,831.
- U.S. Pat. No. 5,76,5396 and U.S. Pat. No. 5,251,451 describe installations according to the preamble of
claim 1. - However this invention proposes to vaporise the deconcentration purge of a vaporiser in an exchanger in order to recover the refrigeration, this vaporiser being the exchanger making it possible to vaporise a liquid of the apparatus under pressure in order to produce a pressurised gaseous product.
- It is desirable to send the purge to a storage of pressurised gases making it possible to maintain stable production in terms of flow as well as in terms of pressure.
- According to an embodiment of the invention, an apparatus for separating air is provided comprising a double column comprising a medium-pressure column and a low-pressure column, a main exchanger, a vaporiser, a main compressor, means for sending all of the air to be treated in the double column to the main compressor in order to produce air substantially at the pressure P1 of the medium-pressure column, means for sending a portion of the air substantially at a high pressure P2 to the main exchanger and then to the vaporiser, a pipe for sending air at least partially condensed in the vaporiser to at least one of the columns, a pipe for sending air at the pressure P1 to the medium-pressure column, means of pressurising, a pump, a pipe for withdrawing the liquid oxygen from the low-pressure column and for sending it to the means of pressurising, a pipe for sending liquid oxygen that has been pressurised at a pressure below 9 bar abs from the means of pressurising to the vaporiser, a pipe for sending gaseous oxygen from the vaporiser to the main exchanger to be heated in order to form a first flow of gaseous oxygen, a purge pipe for sending liquid purge oxygen from the vaporiser to the pump in order to pressurise it characterised in that the purge pipe is not connected to a purge liquid storage and in that it comprises a pipe for sending pressurised oxygen from the pump to an exchanger in order to be vaporised, with the exchanger being connected to a pipe for compressed air connected to the main compressor and to a pipe connected to the double column, in order to form a second flow of gaseous oxygen.
- Optionally:
-
- the exchanger connected to the oxygen purge pipe is the main exchanger.
- the exchanger connected to the oxygen purge pipe is an exchanger separate from the main exchanger.
- the exchanger comprises passages connected to a supply air inlet pipe and passages connected to a liquid refrigerant inlet pipe, possibly coming from the double column.
- the apparatus comprises a storage of pressurised gases connected to the purge oxygen vaporisation exchanger in order to collect the gaseous oxygen.
- According to another embodiment of the invention, a method is provided for separating air in an apparatus comprising a double column comprising a medium-pressure column and a low-pressure column, a main exchanger, a vaporiser, a main compressor, means of pressurising, a pump, wherein all the air to he treated is sent in the double column to the main compressor in order to produce air substantially at the pressure P1 of the medium-pressure column, a portion of the air substantially at a high pressure P2 is sent to the main exchanger and then to the vaporiser, air at least partially condensed in the vaporiser is sent to at least one of the columns, air at the pressure P1 is sent to the medium-pressure column, liquid oxygen is withdrawn from the low-pressure column and it is pressurised, the liquid oxygen that has been pressurised is sent at a pressure below 5 bar abs to the vaporiser, a first flow of gaseous oxygen is sent from the vaporiser to the main exchanger to be heated and liquid purge oxygen of the vaporiser is pressurised in the pump characterised in that the liquid purge oxygen is pressurised without having been stored and is then vaporised in an exchanger through exchange of heat with the air, compressed in the main compressor and intended for the double column, in order to form a second flow of gaseous oxygen.
- Optionally:
-
- the purge oxygen is pressurised at a pressure of at, least 10 bars abs, more preferably at least 15 bars abs, even at least 20 bars abs in the second pump.
- the purge oxygen is vaporised in the main exchanger.
- the purge oxygen is vaporised in an exchanger other than the main exchanger.
- the second flow of gaseous oxygen is sent to a storage of pressurised gases and is used for backup production.
- a variable quantity of the second flow of gaseous oxygen is mixed with the first flow in order to produce a substantially constant mixed flow.
- the liquid oxygen withdrawn from the low-pressure column contains at least 80% mol. oxygen
- the liquid oxygen withdrawn from the low-pressure column constitutes the only flow containing at least 80% mol. oxygen withdrawn from the low-pressure column.
- the liquid oxygen withdrawn from the low-pressure column contains at most 98% mol. oxygen.
- These and other features, aspects, and advantages of the present invention will become better understood with regard to the following description, claims, and accompanying drawings. It is to be noted, however, that the drawings illustrate only several embodiments of the invention and are therefore not to be considered limiting of the invention's scope as it can admit to other equally effective embodiments.
-
FIG. 1 shows an embodiment of the present invention. -
FIG. 2 shows another embodiment of the present invention. - The invention shall be described in more detail by referring to the figures which show apparatuses for separating air according to the invention.
- In
FIG. 1 , the apparatus comprises anexchange line 21 and a double column constituted of a medium-pressure column 27 and a low-pressure column 29. - All of the air I is compressed in the main compressor 2 in order to produce air at the pressure P1 substantially equal to the pressure of the medium-
pressure column 27. The air at the pressure P1 is cooled in a cooler 7, purified in a purification unit 9 and divided into three fractions. The first fraction 11 is supercharged in a supercharger, able to be constituted of the last stage of the main compressor, with this last stage being part of the second portion of the compressor. The pressure P1 is below 5 bars abs, even 4.5 bar abs, preferably below 4 bar, and even below 3.5 bar abs. - The first fraction 11 is brought to a pressure P2 by the
booster 5 or anindependent compressor 5 and cooled at this pressure in a cooler (not shown) before being sent to theexchange line 21. The exchange line is comprised of a brazed-plate aluminium indirect heat exchanger. The fraction 11 is then sent in gaseous form to a vaporiser 41 where it is condensed at least partially before being expanded and sent to the medium-pressure column 27. The pressure P2 is below 15 bar abs, preferably below 10 bar, and even below 6 bar abs. The fraction 11. is less than half of theflow 1, and preferably less than a third of theflow 1. - The second fraction 1.3 at the pressure P1 is cooled entirely in the
exchange line 21 and is divided into two flows. Thefirst flow 23 is sent to atank reboiler 33 from the low-pressure column 29 where it is condensed at least partially and is sent to the medium-pressure column, mixed with the flow 11. Thesecond flow 25 is sent in gaseous form to the median-pressure column 27. - The
third fraction 15 is pressurized in a boostercharger 17, partially cooled in theexchange line 21, withdrawn from the exchange line at an intermediary level of the latter and expanded in aturbine 19 coupled to the supercharger 17 before being sent to the low-pressure column 29. - A flow of oxygen-rich liquid 55, an
intermediate flow 53 and a flow of nitrogen-rich liquid 51 are withdrawn from the medium-pressure column 27, cooled in theexchanger 31, expanded and sent to different levels of the low-pressure column 29. - Medium-pressure gaseous nitrogen 49 is condensed in an
intermediate vaporiser 35 of the low-pressure column 29 and sent as a reflux at the head of themedium pressure column 27. Another flow of medium-pressure gaseous nitrogen 47 is heated in the exchange line. -
Liquid oxygen 37, containing at least 80% mol. oxygen and possibly at most 98% mol. oxygen, is withdrawn from the tank of the low-pressure column 29, pressurised by apump 39 at a pressure below 9 bars abs, even below 5 bars abs and sent to the vaporiser 41. Other than a liquid purge 43, the oxygen is vaporised in the vaporiser 41 by exchange of heat with the fraction of air 11 at the pressure P2. This oxygen then forms the first flow of pressurisedgaseous oxygen 45 which is heated in theexchange line 21. The fraction of air 11 is partially condensed and is sent to the double column. - The purge liquid 43 is pressurised to a pressure of at least 10 bars abs, or at least 15 bar abs, even at least 20 bars abs in a
pump 63 then is vaporised in theexchange line 21. The second gaseous flow produced as such 59 is sent to a storage of pressurised gases 3 and expanded in order to be mixed with theflow 45 via thepipe 61. - Here the vaporisation of purge liquid is carried by using primarily substantial heat, in such a way that no airflow exiting the
exchanger 21 is fully condensed, or even is condensed. - Alternatively as shown in
FIG. 2 , the pressurised purge liquid 43 can be vaporised in anauxiliary exchanger 21A, separate from the exchange line, against an airflow 25A and with a liquid refrigerant, for example a flow of nitrogen 57A heated with the method of separating. - The flow 25A cooled in the
exchanger 21A is mixed with the cooledflow 25 and the flow of nitrogen 57A heated in theexchanger 21A is mixed with the heated flow 57. - The second flow of
gaseous oxygen 59, 61 formed by the vaporisation can be used as a backup gas during an interruption of the production ofgaseous oxygen 45. - As such the only airflow which is used to vaporise the purge oxygen 43 remains in gaseous form in the
exchanger 21A and the vaporisation is carried out by substantial heat exchange. - The pressurisation by the
pump 39 and/or 63 can be replaced with a hydrostatic pressurisation in all of the eases described. - For all of the figures, a variable quantity of the second flow of gaseous oxygen is mixed with the first flow in order to produce a substantially constant mixed flow.
- This variable quantity of the vaporised purge liquid can be mixed with the
first flow 45 in order to smooth. out the variations of flow, due, for example to variations of the pressure of the oxygen network. - By detecting a reduction in pressure in the
line 45, due, for example to an increased oxygen demand, oxygen can be expanded and sent from storage 3 to theline 45 via thepipe 61. - In the event of a breakdown of the apparatus for separating air, the flow of
oxygen 45 will be reduced or will be nonexistent. In this case, the flow ofoxygen 63 from storage 3 can supply a client, the time for a backup vaporiser to be operational in order to prevent any stoppage of production. - The
flow 37 is the only flow containing more than 60% mol. oxygen withdrawn from the low-pressure column. - The storage 3 operates at a pressure that is higher than the
flow 45. - While the invention has been described in conjunction with specific embodiments thereof, it is evident that many alternatives, modifications, and variations will be apparent to those skilled in the art in light of the foregoing description. Accordingly, it is intended to embrace all such alternatives, modifications, and variations as fall within the spirit and broad scope of the appended claims. The present invention may suitably comprise, consist or consist essentially of the elements disclosed and may be practiced in the absence of an element not disclosed. Furthermore, if there is language referring to order, such as first and second, it should be understood in an exemplary sense and not in a limiting sense. For example, it can be recognized by those skilled in the art that certain steps can be combined into a single step.
- The singular forms “a”, an and “the” include plural referents, unless the context clearly dictates otherwise.
- “Comprising” in a claim is an open transitional term which means the subsequently identified claim elements are a nonexclusive listing (i.e., anything else may be additionally included and remain within the scope of “comprising”). “Comprising” as used herein may be replaced by the more limited transitional terms “consisting essentially of” and “consisting of” unless otherwise indicated herein.
- “Providing” in a claim is defined to mean furnishing, supplying, making available, or preparing something. The step may be performed by any actor in the absence of express language in the claim to the contrary a range is expressed, it is to be understood that another embodiment is from the one.
- Optional or optionally means that the subsequently described event or circumstances may or may not occur. The description includes instances where the event or circumstance occurs and instances where it does not occur.
- Ranges may be expressed herein as from about one particular value, and/or to about another particular value. When such particular value and/or to the other particular value, along with all combinations within said range.
- All references identified herein are each hereby incorporated by reference into this application in their entireties, as well as for the specific information for which each is cited.
Claims (19)
1-15. (canceled)
16. An apparatus for separating air, the apparatus comprising:
a double column comprising a medium-pressure column and a low-pressure column;
a main exchanger;
a vaporizer; a main compressor;
means for sending all of the air to be treated in the double column to the main compressor in order to produce air substantially at the pressure P1 of the medium-pressure column;
means for sending a portion of the air substantially at a high pressure P2 to the main exchanger and then to the vaporizer;
a pipe for sending air at least partially condensed in the vaporizer to at least one of the columns;
a pipe for sending air at the pressure P1 to the medium-pressure column;
means of pressurizing;
a pump;
a pipe for withdrawing liquid oxygen from the low-pressure column and for sending it to the means of pressurizing;
a pipe for sending the liquid oxygen that has been pressurized at a pressure below 9 bar abs from the means of pressurizing to the vaporizer;
a pipe for sending gaseous oxygen from the vaporizer to the main exchanger to be heated for forming a first flow of gaseous oxygen;
a purge pipe for sending the liquid purge oxygen from the vaporizer to the pump in order to pressurize the liquid purge oxygen; and
a pipe for sending the pressurized oxygen from the pump to an exchanger to be vaporized,
wherein the purge pipe is not connected to a purge liquid storage, and
wherein the exchanger is connected to a pipe for compressed air connected to the main compressor and to a pipe connected to the double column, thereby forming a second flow of gaseous oxygen.
17. The apparatus as claimed in claim 16 , wherein the exchanger connected to the oxygen purge pipe is the main exchanger.
18. The apparatus as claimed in claim 16 , wherein the exchanger connected to the oxygen purge pipe is an exchanger separate from the main exchanger.
19. The apparatus as claimed in claim 17 , wherein the exchanger comprises passages connected to a supply air inlet pipe and passages connected to a liquid refrigerant inlet pipe, possibly coming from the double column.
20. The apparatus as claimed in claim 16 further comprising a storage of pressurized gases connected to the exchanger for the vaporization of purge oxygen in order to collect the gaseous oxygen.
21. A method for separating air in an apparatus comprising a double column having a medium-pressure column and a low-pressure column; a main exchanger; a vaporizer; a main compressor; means of pressurizing; a pump; the method comprising the steps of:
sending all of the air to he treated in the double column to the main compressor to produce air substantially at the pressure P1 of the medium-pressure column;
sending a portion of the air substantially at a high pressure P2 to the main exchanger and then to the vaporizer;
sending air at least partially condensed in the vaporizer to at least one of the columns;
sending air at the pressure P1 to the medium-pressure column;
withdrawing and pressurizing liquid oxygen from the low-pressure column to a pressure below 5 bar abs;
sending the liquid oxygen that has been pressurized at a pressure below 5 bar abs to the vaporizer;
sending a first flow of gaseous oxygen from the vaporizer to the main exchanger to be heated; and
pressurizing the liquid purge oxygen of the vaporizer in the pump, wherein the liquid purge oxygen is pressurized without having been stored and is then vaporized in an exchanger via heat exchange with the air, compressed in the main compressor and intended for the double column, thereby forming a second flow of gaseous oxygen.
22. The method as claimed in claim 21 further comprising pressurizing the purge oxygen at a pressure of at least 10 bars abs in the second pump.
23. The method as claimed in claim 21 further comprising pressurizing the purge oxygen at a pressure of at least 15 bars abs in the second pump.
24. The method as claimed in claim 21 further comprising pressurizing the purge oxygen at a pressure of at least 20 bars abs in the second pump.
25. The method as claimed in claim 21 further comprising vaporizing the purge oxygen in the main exchanger.
26. The method as claimed in claim 21 further comprising vaporizing the purge oxygen in an exchanger other than the main exchanger.
27. The method as claimed in claim 21 further comprising sending the second flow of gaseous oxygen to a storage of pressurized gases to be used for backup production.
28. The method as claimed in claim 21 further comprising mixing a variable quantity of the second flow of gaseous oxygen with the first flow of gaseous oxygen to produce a substantially constant mixed flow.
29. The method as claimed in claim 21 , wherein the liquid oxygen withdrawn from the low-pressure column contains at least 80% mol. oxygen.
30. The method as claimed in claim 29 , wherein the liquid oxygen withdrawn from the low-pressure column constitutes the only flow containing at least 80% mol. oxygen withdrawn from the low-pressure column.
31. The method as claimed in claim 21 , wherein the liquid oxygen withdrawn from the low-pressure column contains at most 98% mol. oxygen.
32. The method as claimed in claim 21 , further comprising an absence of fully condensing airflow in the exchanger wherein the purge oxygen is vaporized.
33. The method as claimed in claim 21 , further comprising an absence condensing airflow in the exchanger wherein the purge oxygen is vaporized.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR1152272 | 2011-03-18 | ||
FR1152272A FR2972794B1 (en) | 2011-03-18 | 2011-03-18 | APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
PCT/FR2012/050500 WO2012127148A2 (en) | 2011-03-18 | 2012-03-09 | Device and method for separating air by cryogenic distillation |
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Publication Number | Publication Date |
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US20130340476A1 true US20130340476A1 (en) | 2013-12-26 |
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US14/003,902 Abandoned US20130340476A1 (en) | 2011-03-18 | 2012-03-09 | Apparatus and method for separating air by cryogenic distillation |
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US (1) | US20130340476A1 (en) |
EP (1) | EP2686628B1 (en) |
AU (1) | AU2012230171B2 (en) |
CA (1) | CA2828716C (en) |
ES (1) | ES2859549T3 (en) |
FR (1) | FR2972794B1 (en) |
WO (1) | WO2012127148A2 (en) |
ZA (1) | ZA201306723B (en) |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2015127648A1 (en) * | 2014-02-28 | 2015-09-03 | Praxair Technology, Inc. | Pressurized product stream delivery |
Families Citing this family (1)
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JP5997105B2 (en) * | 2013-06-05 | 2016-09-28 | 神鋼エア・ウォーター・クライオプラント株式会社 | Air separation method |
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- 2012-03-09 ES ES12714763T patent/ES2859549T3/en active Active
- 2012-03-09 US US14/003,902 patent/US20130340476A1/en not_active Abandoned
- 2012-03-09 WO PCT/FR2012/050500 patent/WO2012127148A2/en active Application Filing
- 2012-03-09 EP EP12714763.5A patent/EP2686628B1/en active Active
- 2012-03-09 AU AU2012230171A patent/AU2012230171B2/en active Active
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2013
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Also Published As
Publication number | Publication date |
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FR2972794A1 (en) | 2012-09-21 |
WO2012127148A2 (en) | 2012-09-27 |
AU2012230171B2 (en) | 2017-03-30 |
EP2686628A2 (en) | 2014-01-22 |
CA2828716C (en) | 2020-02-25 |
EP2686628B1 (en) | 2021-01-13 |
CN104067079A (en) | 2014-09-24 |
ES2859549T3 (en) | 2021-10-04 |
WO2012127148A3 (en) | 2014-12-04 |
FR2972794B1 (en) | 2015-11-06 |
ZA201306723B (en) | 2015-03-25 |
AU2012230171A1 (en) | 2013-10-10 |
CA2828716A1 (en) | 2012-09-27 |
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Owner name: L'AIR LIQUIDE, SOCIETE ANONYME POUR L'ETUDE ET L'E Free format text: ASSIGNMENT OF ASSIGNORS INTEREST;ASSIGNORS:COGNARD, MARIE;DAVIDIAN, BENOIT;DUBETTIER-GRENIER, RICHARD;REEL/FRAME:031274/0854 Effective date: 20130812 |
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STCB | Information on status: application discontinuation |
Free format text: ABANDONED -- FAILURE TO RESPOND TO AN OFFICE ACTION |