EP2591301A2 - Vorrichtung und verfahren zur lufttrennung durch kryogene destillation - Google Patents

Vorrichtung und verfahren zur lufttrennung durch kryogene destillation

Info

Publication number
EP2591301A2
EP2591301A2 EP11728894.4A EP11728894A EP2591301A2 EP 2591301 A2 EP2591301 A2 EP 2591301A2 EP 11728894 A EP11728894 A EP 11728894A EP 2591301 A2 EP2591301 A2 EP 2591301A2
Authority
EP
European Patent Office
Prior art keywords
flow
oxygen
liquid
rich
storage
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP11728894.4A
Other languages
English (en)
French (fr)
Other versions
EP2591301B1 (de
Inventor
Benoît DAVIDIAN
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Original Assignee
Air Liquide SA
LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Air Liquide SA, LAir Liquide SA pour lEtude et lExploitation des Procedes Georges Claude filed Critical Air Liquide SA
Publication of EP2591301A2 publication Critical patent/EP2591301A2/de
Application granted granted Critical
Publication of EP2591301B1 publication Critical patent/EP2591301B1/de
Active legal-status Critical Current
Anticipated expiration legal-status Critical

Links

Classifications

    • 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
    • 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
    • F25J3/0204—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 feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
    • F25J3/04187—Cooling of the purified feed air by recuperative heat-exchange; Heat-exchange with product streams
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • 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
    • F25J3/04412—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
    • 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
    • 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
    • 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
    • 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
    • F25J2215/02—Mixing or blending of fluids to yield a certain product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • 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
    • 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

  • the present invention relates to an apparatus and method for air separation by cryogenic distillation.
  • a purge liquid is sent to a storage, and a portion of storage liquid is sent into an exchanger to be mixed with oxygen gas.
  • the storage is also powered by liquid transported by a truck, so it is a liquid oxygen injection with a supplement of external liquid, thereby vaporizing the purge with heated oxygen gas.
  • a storage is supplied by a purge flow from the tank of the low pressure column in the event of reduction of the production of the column system, a storage flow is withdrawn from the storage which is vaporized in a emergency vaporizer.
  • the purge can compensate the evaporation losses in the storage and the excess is vaporized in the system of the emergency vaporization (without recovery of frigories in the cold box).
  • it is intended to send a purge flow to a storage of liquid oxygen, possibly using a pump depending on its pressure.
  • a flow of oxygen-rich liquid having a nominal flow rate is withdrawn from the low-pressure column, vaporized in a main evaporator to form a gaseous product, and an oxygen-rich liquid purge flow rate of not more than 2% of nominal output flow of the oxygen-rich flow of the vaporizer,
  • the oxygen-rich liquid purge flow rate of the low pressure column vessel or the vaporizer is sent into the storage system permanently or episodically, outside the stopping and starting periods of the column system.
  • the flow rate having a nominal flow rate is a flow rate of gas withdrawn from the low pressure column and the purge flow rate constitutes the only oxygen-rich flow rate withdrawn from the column system.
  • the storage is filled with liquid from a tank of at least one column of the column system.
  • a flow of oxygen rich gas having a nominal flow rate is withdrawn from the low pressure column in order to form a gaseous product, and an oxygen-rich liquid purge flow rate is drawn off in the bottom of the low pressure column, the purge flow being richer; in oxygen and heavy impurities that the flow having the nominal flow and constituting at most 2% of the nominal rate of production of oxygen-rich flow.
  • a flow of oxygen rich liquid having a nominal flow rate is withdrawn from the low pressure column, it is vaporized in a main vaporizer to form a gaseous product and an oxygen-rich liquid purge flow rate is drawn up constituting at most 2% of the flow rate; nominal flow rate of the oxygen-rich flow of the vaporizer.
  • the delivery of the product from the storage to the shaker vaporizer is only triggered if the customer's needs increase or if the production is reduced. column system.
  • the emergency vaporizer has a vaporization function of the overflow in the storage.
  • an apparatus for separating air by cryogenic distillation comprising a system of columns comprising a medium pressure column and a low pressure column, a storage, a backup vaporizer and either
  • a main vaporizer means for withdrawing from the low pressure column a flow of oxygen-rich liquid having a nominal flow rate and sending it to the main vaporizer, means for withdrawing a gaseous product formed by vaporization of the liquid flow, means for withdrawing an oxygen-rich liquid purge flow rate constituting not more than 2% of the nominal flow rate for producing the oxygen-rich flow rate of the vaporizer,
  • sensing and control means for detecting the liquid level in the storage and for triggering, if the level exceeds a threshold corresponding to the maximum capacity, withdrawing a liquid flow of the storage constituting at most 2% of the nominal flow rate of production of the flow rich in oxygen and the sending of this flow rate to the backup vaporizer to constitute a part of the gaseous product, these detection and control means being able to detect if the level of liquid in the storage is below the threshold and, in this case, triggering the sending of the liquid purge flow to the storage and the prevention of sending the liquid from the storage to the emergency vaporizer except in the case reducing the production of the column system or increasing the need of a customer for the gaseous product.
  • the device does not include a means of spraying purge liquid apart from the emergency vaporizer.
  • the apparatus comprises means for withdrawing from the low pressure column a flow of oxygen-rich gas having a nominal flow rate to form a gaseous product and means for withdrawing an oxygen-rich liquid purge flow rate in the bottom of the low pressure column; , the purge flow rate being richer in oxygen and heavy impurities than the flow rate having the nominal flow rate and constituting not more than 2% of the nominal rate of production of the oxygen-rich flow.
  • the device includes
  • a main vaporizer means for extracting from the low pressure column a flow of oxygen-rich liquid having a nominal flow rate and sending it to the main vaporizer, means for withdrawing a gaseous product formed by vaporization of the liquid flow rate and means for withdrawing an oxygen-rich liquid purge flow rate constituting not more than 2% of the nominal output flow rate of the oxygen-rich flow of the vaporizer.
  • the transfer pump may also be that used for the transfer of liquid oxygen production, if any.
  • the storage of liquid oxygen is filled with oxygen of "commercial industrial” quality which is therefore “pure” (99.5 mol%).
  • oxygen of "commercial industrial” quality which is therefore “pure” (99.5 mol%).
  • Sending a purge liquid with a mean purity lower than that of the storage liquid will slightly reduce the purity of liquid contained in the storage, which will nonetheless be at a higher average content than the customer demand.
  • a flow rich in oxygen, gaseous or liquid, contains at least 75 mol%. oxygen.
  • a flow of compressed and purified air 1 is cooled in a heat exchanger 3 and divided into three.
  • a flow 7 is withdrawn from the exchanger at an intermediate level, expanded in a turbine 9 and sent to a low pressure column 13 of a double column in gaseous form.
  • Another flow 5 after being supercharged in the compressor A liquefies in the exchanger 3, is expanded in a valve 1 1 and sent to the medium pressure column 13.
  • a third flow B sent directly into the medium pressure column.
  • Flow rates enriched with nitrogen and oxygen are sent from the medium pressure column to the low pressure column in a known manner.
  • the liquid oxygen accumulates around the reboiler 17.
  • a flow of liquid oxygen 19 containing less than 98% of oxygen is withdrawn from the tank of the low pressure column 15 and pressurized by a pump 23 up to 2 bars, alternatively the compression can be hydrostatic.
  • Part of the oxygen at this pressure is sent to a vaporizer 24 where it vaporizes by heat exchange with a portion of the supply air (5 or B) which is then sent to the column.
  • This vaporized flow rate constitutes the gaseous production of the column system in normal operation and is produced with a nominal flow rate.
  • a purge flow 121 containing impurities is withdrawn from the vaporizer
  • This flow rate is purer in oxygen than the flow rate 19.
  • the vaporized oxygen continues to heat up in the exchanger 3 as the flow rate 27 of low pressure oxygen.
  • the rest of the oxygen is pressurized to a pressure of 10 bar in a pump 25 and vaporizes in the exchanger 3 as flow 29.
  • all the oxygen can be vaporized to the lower pressure and the flow 29 does not exist.
  • a first conduit connects the vaporizer 24 with the storage 31 to bring the purge liquid 121 permanently or episodically, unless the column system does not work.
  • the storage 31 supplies a backup vaporizer 37 with liquid oxygen 35.
  • the purge liquid can be sent episodically, that is to say that the liquid is withdrawn from the vaporizer periodically, in a cycle, in order to have quantities of liquid allowing a correct analysis.
  • Oxygen is vaporized in the emergency vaporizer 37 in large quantities, when the customer's needs are particularly high or when the air separation device does not operate at full speed, in case of failure, for example.
  • an oxygen-rich liquid flow constituting less than 2% of the nominal oxygen gas flow rate 19 and preferably about 1% of the nominal flow is sent to the storage.
  • This liquid flow rate is sent to the backup vaporizer only if the level in the storage exceeds a threshold, this threshold being ordinarily that of the maximum capacity of the storage 31.
  • this flow sent to the backup vaporizer constitutes the overflow of the storage 31.
  • the vaporized oxygen is sent to the customer.
  • the storage 31 is filled by sending the liquid 121 there.
  • the liquid in the storage comes from a tanker 61 or from the apparatus itself by the flow 21, which can be diverted to storage punctually.
  • the liquid in the storage from the truck has a purity of 99.5 mol%.
  • the liquid 121 may be purer, as pure or less pure than the liquid from the tanker truck.61.
  • liquids accumulated in the bottom of the low pressure and / or medium pressure column in the lines 21 and 51 will obviously have a purity lower than that of the liquid from the truck 61 or that of the liquid 121. In some cases, the customer can withstand a short-term reduction of purity of the vaporized liquid in the backup vaporizer.
  • a valve 41 makes it possible to regulate the flow rates of these accumulated liquids sent to the storage 31.
  • a flow of compressed and purified air 1 is cooled in a heat exchanger 3 and divided into two.
  • a flow 7 is withdrawn from the exchanger at an intermediate level, expanded in a turbine 9 and sent to a low pressure column 13 of a double column in gaseous form.
  • Another flow 5 is cooled in the heat exchanger 3, and sent to the medium pressure column 13.
  • Flow rates enriched with nitrogen and oxygen are sent from the medium pressure column to the low pressure column in a known manner.
  • the liquid oxygen accumulates around the reboiler 17.
  • a flow of gaseous oxygen 19 containing 98% of oxygen is withdrawn from the tank of the low pressure column 15 and is heated in the exchanger 3 as flow 27 low pressure oxygen before undergoing a possible compression.
  • a purge flow 21 containing impurities is withdrawn from the tank of the column 15 continuously to avoid the accumulation of impurities in the bottom of the column. This liquid withdrawal is the only oxygen-rich withdrawal of the column system.
  • a first conduit connects the LP column vessel with the storage 31 to bring the purge liquid 21 continuously (either continuously or in regular batches), unless the column system does not work.
  • the storage 31 supplies a backup vaporizer 37 with liquid oxygen 35.
  • Oxygen is vaporized in the emergency vaporizer 37 in large quantities, when the customer's needs are particularly high or when the air separation device does not operate at full speed, in case of failure, for example.
  • an oxygen-rich liquid flow constituting less than 2% of the nominal oxygen gas flow rate 19 and preferably about 1% of the nominal flow is sent to the storage.
  • This liquid flow rate is sent to the backup vaporizer if the level in the storage exceeds a threshold, this threshold being ordinarily that of the maximum capacity of the storage 31.
  • this flow sent to the backup vaporizer constitutes the overflow of the storage 31.
  • Vaporized oxygen is sent to the customer
  • the storage 31 is filled by sending the liquid 21. In normal operation therefore, the storage liquid is not sent to the backup vaporizer, if the maximum level is not reached.
  • the triggering of the sending of the storage to the backup vaporizer may be necessary, in the event of a reduction in the production of the column system or an increase in the customer's needs.
  • the purge flow 21 has a higher oxygen molar purity than the flow rate 19.
  • liquid in the storage comes from a tank truck 61 or the device itself by a liquid flow drawn off punctually (not shown), which can be sent to storage.
  • the liquid in the storage from the truck has a purity of 99.5 mol%.
  • a pump may be needed to send the purge liquid 21 to the storage.
  • the purge flow 21 may be purer, as pure or less pure than the liquid supplying the storage from the tanker 61 for example.
  • the liquid from the storage 31 can be vaporized in a backup vaporizer 37 and sent to a customer in case of failure of the distillation apparatus and / or if production of the distillation apparatus is insufficient to supply the customer.

Landscapes

  • 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)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
EP11728894.4A 2010-07-05 2011-07-05 Vorrichtung und verfahren zur lufttrennung durch kryogene destillation Active EP2591301B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
FR1055423 2010-07-05
FR1055421 2010-07-05
PCT/EP2011/061279 WO2012004242A2 (fr) 2010-07-05 2011-07-05 Appareil et procede de separation d'air par distillation cryogenique

Publications (2)

Publication Number Publication Date
EP2591301A2 true EP2591301A2 (de) 2013-05-15
EP2591301B1 EP2591301B1 (de) 2020-09-02

Family

ID=45441586

Family Applications (2)

Application Number Title Priority Date Filing Date
EP11728893.6A Withdrawn EP2591300A2 (de) 2010-07-05 2011-07-05 Verfahren und vorrichtung zur trennung von luft durch kryogene destillation
EP11728894.4A Active EP2591301B1 (de) 2010-07-05 2011-07-05 Vorrichtung und verfahren zur lufttrennung durch kryogene destillation

Family Applications Before (1)

Application Number Title Priority Date Filing Date
EP11728893.6A Withdrawn EP2591300A2 (de) 2010-07-05 2011-07-05 Verfahren und vorrichtung zur trennung von luft durch kryogene destillation

Country Status (5)

Country Link
US (2) US9581386B2 (de)
EP (2) EP2591300A2 (de)
CN (2) CN103282732B (de)
ES (1) ES2820436T3 (de)
WO (2) WO2012004242A2 (de)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105264317B (zh) * 2013-04-18 2019-02-12 林德股份公司 空气低温分离的改造装置、改造系统以及改造低温空气分离系统的方法
FR3084736B1 (fr) * 2018-08-01 2022-04-15 Air Liquide Procede et appareil de production d'argon par distillation cryogenique de l'air
DE102019000335A1 (de) 2019-01-18 2020-07-23 Linde Aktiengesellschaft Verfahren zur Bereitstellung von Luftprodukten und Luftzerlegungsanlage
FR3095153B1 (fr) * 2019-04-18 2021-11-26 Air Liquide France Ind Procédé d'alimentation en fluide cryogénique d'une machine d'usinage

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GB2125949B (en) * 1982-08-24 1985-09-11 Air Prod & Chem Plant for producing gaseous oxygen
DE3913880A1 (de) * 1989-04-27 1990-10-31 Linde Ag Verfahren und vorrichtung zur tieftemperaturzerlegung von luft
FR2652887B1 (fr) * 1989-10-09 1993-12-24 Air Liquide Procede et installation de production d'oxygene gazeux a debit variable par distillation d'air.
FR2699992B1 (fr) * 1992-12-30 1995-02-10 Air Liquide Procédé et installation de production d'oxygène gazeux sous pression.
FR2706195B1 (fr) * 1993-06-07 1995-07-28 Air Liquide Procédé et unité de fourniture d'un gaz sous pression à une installation consommatrice d'un constituant de l'air.
EP0793069A1 (de) * 1996-03-01 1997-09-03 Air Products And Chemicals, Inc. Mit einem Aufkochkompressor versehener Generator für Sauerstoff von zwei Reinheitsgraden
FR2751737B1 (fr) * 1996-07-25 1998-09-11 Air Liquide Procede et installation de production d'un gaz de l'air a debit variable
JPH10132458A (ja) * 1996-10-28 1998-05-22 Nippon Sanso Kk 酸素ガス製造方法及び装置
US5907959A (en) * 1998-01-22 1999-06-01 Air Products And Chemicals, Inc. Air separation process using warm and cold expanders
WO1999039143A1 (de) * 1998-01-30 1999-08-05 Linde Aktiengesellschaft Verfahren und vorrichtung zum verdampfen von flüssigem sauerstoff
CA2319552C (en) * 1998-02-04 2004-04-20 Texaco Development Corporation Combined cryogenic air separation with integrated gasifier
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DE19852020A1 (de) * 1998-08-06 2000-02-10 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
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Also Published As

Publication number Publication date
CN103282733A (zh) 2013-09-04
WO2012004242A3 (fr) 2013-11-28
WO2012004242A2 (fr) 2012-01-12
WO2012004241A2 (fr) 2012-01-12
EP2591300A2 (de) 2013-05-15
WO2012004241A3 (fr) 2013-11-28
CN103282733B (zh) 2015-11-25
US20130098106A1 (en) 2013-04-25
US9581386B2 (en) 2017-02-28
CN103282732A (zh) 2013-09-04
EP2591301B1 (de) 2020-09-02
CN103282732B (zh) 2016-08-03
ES2820436T3 (es) 2021-04-21
US20130133364A1 (en) 2013-05-30

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