US20010003909A1 - Process and installation for separation of air by cryogenic distillation - Google Patents
Process and installation for separation of air by cryogenic distillation Download PDFInfo
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- US20010003909A1 US20010003909A1 US09/725,462 US72546200A US2001003909A1 US 20010003909 A1 US20010003909 A1 US 20010003909A1 US 72546200 A US72546200 A US 72546200A US 2001003909 A1 US2001003909 A1 US 2001003909A1
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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
- F25J3/04642—Recovering noble gases from air
- F25J3/04648—Recovering noble gases from air argon
- F25J3/04654—Producing crude argon in a crude argon column
- F25J3/04709—Producing crude argon in a crude argon column as an auxiliary column system in at least a dual pressure main column system
- F25J3/04715—The auxiliary column system simultaneously produces 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
- F25J3/0446—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 the heat generated by mixing two different phases
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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
- F25J3/0446—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 the heat generated by mixing two different phases
- F25J3/04466—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 the heat generated by mixing two different phases for producing oxygen as a mixing column overhead gas by mixing gaseous air feed and liquid 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
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04969—Retrofitting or revamping of an existing air fractionation unit
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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
- F25J2200/04—Processes or apparatus using separation by rectification in a dual pressure main column system
- F25J2200/06—Processes or apparatus using separation by rectification in a dual pressure main column system in a classical double column flow-sheet, 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the 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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
- Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y10S62/00—Refrigeration
- Y10S62/923—Inert gas
- Y10S62/924—Argon
Definitions
- the invention relates to a process and a plant for the separation of air by cryogenic distillation.
- it relates to a process for producing pure oxygen using a mixing column and, possibly, for producing argon using an argon column.
- EP-A-0269342 relates to the case in which the argon column is thermally coupled to a mixing column so that the overhead gas of the argon column warms the mixing column.
- U.S. Pat. No. 5,551,258 describes a process in which a mixing column is fed at the top with a liquid containing 55 vol % oxygen, the overhead gas of the mixing column then serving to warm the bottom condenser of the low-pressure column.
- One object of the present invention is to increase the amount of pure gaseous oxygen (containing more than 99.5 mol % oxygen) which can be produced by a double air separation column.
- One object of the invention is an air separation plant for producing an oxygen-rich fluid by cryogenic distillation, comprising:
- a double column comprising at least one medium-pressure column and a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column;
- [0011] means for sending cooled and compressed air to the medium-pressure column
- [0012] means for sending an oxygen-enriched liquid from the medium-pressure column to an injection point of the low-pressure column and means for sending a nitrogen-enriched liquid from the medium-pressure column to the low-pressure column;
- [0013] means for sending gas to the bottom of the mixing column
- [0014] means for sending a second oxygen-enriched liquid from the low-pressure column to the top of the mixing column, this second liquid being less volatile than the gas feeding the bottom of the mixing column;
- [0016] means for sending at least one portion of a gas, possibly the overhead gas, from the mixing column to passages for warming the reboiler,
- the apparatus may include an argon column or simply a vaporiser for vaporizing liquid from the bottom of the medium pressure column by heat exchange with a gas from the low pressure column.
- Preferably it comprises meand for withdrawing the second liquid at a level between the bottom of the low pressure column and the point of removal of the feed to the argon column or the point of removal of the gas sent from the low pressure column to the rich liquid vaporizer.
- the mixing column may be fed at the bottom with any gas more volatile than the liquid oxygen sent to the top of the column.
- Another object of the invention is an air separation plant for producing an oxygen-rich fluid and possibly an argon enriched fluid by cryogenic distillation, comprising:
- a double column comprising a medium-pressure column and a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column;
- [0025] means for sending cooled and compressed air at least to the medium-pressure column
- [0026] means for sending a first oxygen-enriched liquid from the medium-pressure column to the condenser
- [0027] means for withdrawing an argon-enriched gas from a first level of the low-pressure column and means for sending it to the condenser or to the argon column;
- [0028] means for sending an oxygen-enriched liquid from the medium-pressure column to at least one injection point of the low-pressure column and a nitrogen-enriched liquid from the medium-pressure column to the low-pressure column;
- [0029] means for vaporizing oxygen-enriched liquid in the condenser and means for sending at least one portion of the vapour and/or air to the bottom of the mixing column;
- [0030] means for sending a second oxygen-enriched liquid from the low-pressure column to the top of the mixing column, this second liquid being less volatile than the gas feeding the bottom of the mixing column;
- [0033] means for sending at least one portion of a gas, possibly the overhead gas, from the mixing column to passages for warming the reboiler.
- Preferbaly the apparatus comprises means for withdrawing the second liquid is withdrawn from the low-pressure column at a level at least 5 theoretical trays below the point of injection or the lowermost point of injection at a level (still more preferably at least 10 theoretical trays below the point of injection or the lowermost point of injection) and/or about a third of the way up the low-pressure column.
- the overhead gas of the mixing column at least partially condenses in the reboiler and at least part of the condensate is sent to the low pressure column, preferbaly at a level above the first level;
- the apparatus includes a blowing turbine for sending air to the low pressure column or the mixing column;
- the apparatus comprises means for withdrawing gaseous nitrogen from the medium-pressure column as a product.
- Another object of the invention is a process for the separation of air by cryogenic distillation for producing oxygen with a double column comprising:
- a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column
- the second liquid contains less than 5 mol % nitrogen and/or the gas sent from the mixing column to the warming passages contains less than 15 mol % nitrogen.
- Another object of the invention is a process for the separation of air by cryogenic distillation for producing oxygen and possibly argon with a double column comprising:
- a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column;
- a condenser optionally at the top of an argon column, and a mixing column,
- the second liquid contains less than 5 mol. % nitrogen and/or the gas sent from the mixing column to the warming passages contains less than 15 mol. % nitrogen.
- the overhead gas of the mixing column at least partially condenses in the reboiler and the condensate is sent to the low pressure column, possibly at a level above the first level;
- a bottom liquid and/or an intermediate liquid are sent from the mixing column to the double column;
- a gas from the medium-pressure column or air at least partially condenses in other passages for warming the reboiler
- the overhead gas of the mixing column comprises 3 to 5 mol % nitrogen
- the overhead gas of the mixing column comprises at least 93 mol. %, possibly at least 95 mol. % oxygen;
- the liquid sent to the top of the mixing column contains at least 98 mol % oxygen
- the pressure of the mixing column is at between 0,5 and 1 bar above the pressure of the low pressure column.
- the overhead gas of the mixing column may be withdrawn from the top of the mixing column or at most five theoretical trays below the top of the mixing column.
- the plant in FIG. 1 comprises a double column 1 comprising a medium-pressure column 3 and a low-pressure column 5 coupled together via a reboiler 7 .
- the reboiler includes passages for vaporizing liquid and two independent series of warming passages for two different warming gases.
- the low-pressure column operates at between 1.4 and 2.7 bar and the medium-pressure column operates at between 5 and 8 bar.
- the argon column 9 is fed from a first level of the low-pressure column 5 . There is also a mixing column 11 operating at a pressure between 1.9 and 3.7 bar.
- a stream of air 13 is sent to the column 3 and a stream of blown air 14 is sent to the column 5 .
- a stream of liquid 15 containing 40 mol % oxygen is withdrawn from the bottom of the medium-pressure column 3 ; a portion 17 of this liquid feeds the low-pressure column 5 after expansion in a valve and a portion 19 of the liquid is expanded to between 1.7 and 2.2 bar absolute in a valve and sent to the head condenser 21 of the argon column 9 where it at least partially vaporizes.
- the vaporized liquid 23 is sent to the bottom of the mixing column.
- the overhead nitrogen of the low-pressure column at least partially condenses in the bottom reboiler 7 and the condensate is sent to the medium-pressure column and/or the low-pressure column.
- a gas stream 41 containing at least 80 mol % nitrogen is withdrawn as a product from the top of the medium-pressure column and constitutes 10 to 15% of the feed air.
- a stream of nitrogen-enriched liquid 25 containing less than 2 mol % oxygen is sent from the medium-pressure column to the top of the low-pressure column.
- a liquid stream 27 containing less than 5 mol % nitrogen is withdrawn from the bottom of the low-pressure column 5 below the point of withdrawal of the gas 26 intended for the argon column 9 and between 0 and 5 theoretical trays above the bottom of the column and is sent after pumping to between 1.9 and 3.7 bar to the top of the mixing column 11 .
- this stream 27 is mixed with the bottom liquid 29 of the argon column before being pumped and sent to the mixing column.
- a gas stream 31 containing at most 5 mol % nitrogen is sent from the top of the mixing column to the reboiler 7 where it condenses in passages separate from those in which the nitrogen of the medium-pressure column condenses so as to increase the reflux in the bottom of the low-pressure column.
- air or another fluid less volatile than the medium-pressure nitrogen may possibly be condensed therein, provided that it condenses in another condenser of the system, normally above the reboiler.
- a portion of the stream 31 may serve as an oxygen-enriched product.
- the liquid containing 5 mol % nitrogen is sent to the low-pressure column at a level above the point of withdrawal of the stream 26 .
- An intermediate liquid 33 containing 80 mol % oxygen is sent from the mixing column to the low-pressure column 5 .
- the bottom liquid 35 containing 65 mol % oxygen is sent from the mixing column to the low-pressure column 5 .
- a stream 37 containing more than 99.5 mol % oxygen is withdrawn from the bottom of the low-pressure column 5 either in gaseous form or in liquid form.
- the low-pressure column is fed, going from the top downwards, with lean liquid 25 containing less than 1 mol % oxygen, with blowing air 14 , the unvaporized rich liquid 45 from the head condenser of the argon column, the rich liquid 17 , the liquid 35 from the bottom of the mixing column, the intermediate liquid 33 from the mixing column and the recondensed mixture 31 from the reboiler 7 .
- the low-pressure column contains at least 80 theoretical trays and preferably at least 90 theoretical trays.
- the plant in FIG. 2 differs from that in FIG. 1 in that the mixing column is fed at the bottom exclusively with a stream of air possibly coming from a turbine or a supercharger (these not being illustrated).
- the vapour from the condenser 21 of the argon column is sent to the low-pressure column just below the point of injection of the rich liquid 45 .
- the argon column may be omitted or reduced to a simple condenser fed by rich liquid and a gas from the low pressure column, for example having the composition of the feed to the argon column.
- the argon column and/or the low-pressure column may be constructed in two sections in the manner described in EP-A-0628777.
- the medium-pressure and low-pressure columns may be constructed side by side.
- the refrigeration needed for the apparatus may be provided by a blowing turbine and/or a Claude turbine and/or a nitrogen turbine.
- the apparatus may produce liquids and/or gases.
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Abstract
Description
- 1. Field of the invention
- The invention relates to a process and a plant for the separation of air by cryogenic distillation. In particular, it relates to a process for producing pure oxygen using a mixing column and, possibly, for producing argon using an argon column.
- 2. Description of Prior Art
- In EP-A-0229803, the mixing column is fed at the bottom with vaporized rich liquid coming from the head condenser of the argon column.
- EP-A-0269342 relates to the case in which the argon column is thermally coupled to a mixing column so that the overhead gas of the argon column warms the mixing column.
- U.S. Pat. No. 5,551,258 describes a process in which a mixing column is fed at the top with a liquid containing 55 vol % oxygen, the overhead gas of the mixing column then serving to warm the bottom condenser of the low-pressure column.
- One object of the present invention is to increase the amount of pure gaseous oxygen (containing more than 99.5 mol % oxygen) which can be produced by a double air separation column.
- One object of the invention is an air separation plant for producing an oxygen-rich fluid by cryogenic distillation, comprising:
- a double column comprising at least one medium-pressure column and a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column;
- a mixing column;
- means for sending cooled and compressed air to the medium-pressure column;
- means for sending an oxygen-enriched liquid from the medium-pressure column to an injection point of the low-pressure column and means for sending a nitrogen-enriched liquid from the medium-pressure column to the low-pressure column;
- means for sending gas to the bottom of the mixing column;
- means for sending a second oxygen-enriched liquid from the low-pressure column to the top of the mixing column, this second liquid being less volatile than the gas feeding the bottom of the mixing column;
- means for withdrawing an oxygen-rich fluid from the low-pressure column;
- means for sending at least one portion of a gas, possibly the overhead gas, from the mixing column to passages for warming the reboiler,
- characterized in that it includes means for withdrawing the second liquid from the low-pressure column at a level at least 5 theoretical trays below the injection point of the low-pressure column, or possibly at least 10 theoretical trays below the injection point of the low-pressure column and/or about a third of the way up the low pressure column.
- The apparatus may include an argon column or simply a vaporiser for vaporizing liquid from the bottom of the medium pressure column by heat exchange with a gas from the low pressure column.
- Preferably it comprises meand for withdrawing the second liquid at a level between the bottom of the low pressure column and the point of removal of the feed to the argon column or the point of removal of the gas sent from the low pressure column to the rich liquid vaporizer.
- In this case, the mixing column may be fed at the bottom with any gas more volatile than the liquid oxygen sent to the top of the column.
- Another object of the invention is an air separation plant for producing an oxygen-rich fluid and possibly an argon enriched fluid by cryogenic distillation, comprising:
- a double column comprising a medium-pressure column and a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column;
- a condenser, possibly at the top of an argon column;
- a mixing column;
- means for sending cooled and compressed air at least to the medium-pressure column;
- means for sending a first oxygen-enriched liquid from the medium-pressure column to the condenser;
- means for withdrawing an argon-enriched gas from a first level of the low-pressure column and means for sending it to the condenser or to the argon column;
- means for sending an oxygen-enriched liquid from the medium-pressure column to at least one injection point of the low-pressure column and a nitrogen-enriched liquid from the medium-pressure column to the low-pressure column;
- means for vaporizing oxygen-enriched liquid in the condenser and means for sending at least one portion of the vapour and/or air to the bottom of the mixing column;
- means for sending a second oxygen-enriched liquid from the low-pressure column to the top of the mixing column, this second liquid being less volatile than the gas feeding the bottom of the mixing column;
- possibly means for withdrawing an argon-enriched fluid at the top of the argon column;
- means for withdrawing an oxygen-rich fluid from the low-pressure column and
- means for sending at least one portion of a gas, possibly the overhead gas, from the mixing column to passages for warming the reboiler.
- Preferbaly the apparatus comprises means for withdrawing the second liquid is withdrawn from the low-pressure column at a level at least 5 theoretical trays below the point of injection or the lowermost point of injection at a level (still more preferably at least 10 theoretical trays below the point of injection or the lowermost point of injection) and/or about a third of the way up the low-pressure column.
- According to other optional aspects:
- the overhead gas of the mixing column at least partially condenses in the reboiler and at least part of the condensate is sent to the low pressure column, preferbaly at a level above the first level;
- there are means for sending the liquid in the bottom of the argon column to the top of the mixing column;
- there are means for sending a bottom liquid and/or an intermediate liquid from the mixing column to the double column;
- there are at least 80, preferably at least 90, theoretical trays in the low-pressure column;
- there are means for sending air or a gas from the medium-pressure column to other passages for warming the reboiler;
- the apparatus includes a blowing turbine for sending air to the low pressure column or the mixing column;
- the apparatus comprises means for withdrawing gaseous nitrogen from the medium-pressure column as a product.
- Another object of the invention is a process for the separation of air by cryogenic distillation for producing oxygen with a double column comprising:
- a medium-pressure column; and
- a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column,
- comprising the steps of:
- sending cooled and compressed air to the medium-pressure column;
- sending an oxygen-enriched liquid and a nitrogen-enriched liquid from the medium-pressure column to the low-pressure column;
- sending gas to the bottom of the mixing column;
- sending a second oxygen-enriched liquid from the low-pressure column to the top of the mixing column, this second liquid being less volatile than the gas feeding the bottom of the mixing column;
- withdrawing an oxygen-rich fluid from the low-pressure column;
- sending at least one portion of a gas, possibly the overhead gas, from the mixing column to passages for warming the reboiler,
- characterized in that the second liquid contains less than 5 mol % nitrogen and/or the gas sent from the mixing column to the warming passages contains less than 15 mol % nitrogen.
- Another object of the invention is a process for the separation of air by cryogenic distillation for producing oxygen and possibly argon with a double column comprising:
- a medium-pressure column;
- a low-pressure column which includes a reboiler for vaporizing the liquid in the bottom of the low-pressure column; and
- a condenser, optionally at the top of an argon column, and a mixing column,
- comprising the steps of:
- sending cooled and compressed air to at least the medium-pressure column;
- sending a first oxygen-enriched liquid from the medium-pressure column to the head condenser;
- withdrawing an argon-enriched gas from a first level of the low-pressure column and sending it to the condenser or the argon column;
- sending an oxygen enriched liquid and a nitrogen-enriched liquid from the medium-pressure column to the low-pressure column;
- at least partially vaporizing oxygen-enriched liquid in the condenser and sending at least one portion of the vapour and/or air to the bottom of the mixing column;
- sending a second oxygen-enriched liquid from the low-pressure column to the top of the mixing column, this second liquid being less volatile than the gas feeding the bottom of the mixing column;
- possibly withdrawing an argon-enriched liquid from the top of the argon column;
- withdrawing an oxygen-rich fluid from the low-pressure column;
- sending at least one portion of a gas, possibly the overhead gas, from the mixing column to passages for warming the reboiler,
- characterized in that the second liquid contains less than 5 mol. % nitrogen and/or the gas sent from the mixing column to the warming passages contains less than 15 mol. % nitrogen.
- According to other optional aspects:
- the overhead gas of the mixing column at least partially condenses in the reboiler and the condensate is sent to the low pressure column, possibly at a level above the first level;
- at least part of the liquid in the bottom of the argon column is sent to the top of the mixing column;
- a bottom liquid and/or an intermediate liquid are sent from the mixing column to the double column;
- a gas from the medium-pressure column or air at least partially condenses in other passages for warming the reboiler;
- the overhead gas of the mixing column comprises 3 to 5 mol % nitrogen;
- the overhead gas of the mixing column comprises at least 93 mol. %, possibly at least 95 mol. % oxygen;
- the liquid sent to the top of the mixing column contains at least 98 mol % oxygen;
- the pressure of the mixing column is at between 0,5 and 1 bar above the pressure of the low pressure column.
- It will be understood that the overhead gas of the mixing column may be withdrawn from the top of the mixing column or at most five theoretical trays below the top of the mixing column.
- The invention will now be described in greater detail with reference to the figures which diagrammatically illustrate plants according to the invention.
- The plant in FIG. 1 comprises a double column1 comprising a medium-
pressure column 3 and a low-pressure column 5 coupled together via a reboiler 7. - The reboiler includes passages for vaporizing liquid and two independent series of warming passages for two different warming gases.
- The low-pressure column operates at between 1.4 and 2.7 bar and the medium-pressure column operates at between 5 and 8 bar.
- The argon column9 is fed from a first level of the low-pressure column 5. There is also a
mixing column 11 operating at a pressure between 1.9 and 3.7 bar. - A stream of
air 13 is sent to thecolumn 3 and a stream of blownair 14 is sent to the column 5. - A stream of
liquid 15 containing 40 mol % oxygen is withdrawn from the bottom of the medium-pressure column 3; aportion 17 of this liquid feeds the low-pressure column 5 after expansion in a valve and aportion 19 of the liquid is expanded to between 1.7 and 2.2 bar absolute in a valve and sent to thehead condenser 21 of the argon column 9 where it at least partially vaporizes. The vaporizedliquid 23 is sent to the bottom of the mixing column. - The overhead nitrogen of the low-pressure column at least partially condenses in the bottom reboiler7 and the condensate is sent to the medium-pressure column and/or the low-pressure column.
- A
gas stream 41 containing at least 80 mol % nitrogen is withdrawn as a product from the top of the medium-pressure column and constitutes 10 to 15% of the feed air. - A stream of nitrogen-enriched
liquid 25 containing less than 2 mol % oxygen is sent from the medium-pressure column to the top of the low-pressure column. - A
liquid stream 27 containing less than 5 mol % nitrogen is withdrawn from the bottom of the low-pressure column 5 below the point of withdrawal of thegas 26 intended for the argon column 9 and between 0 and 5 theoretical trays above the bottom of the column and is sent after pumping to between 1.9 and 3.7 bar to the top of the mixingcolumn 11. Preferably, thisstream 27 is mixed with thebottom liquid 29 of the argon column before being pumped and sent to the mixing column. - A
gas stream 31 containing at most 5 mol % nitrogen is sent from the top of the mixing column to the reboiler 7 where it condenses in passages separate from those in which the nitrogen of the medium-pressure column condenses so as to increase the reflux in the bottom of the low-pressure column. Instead of this nitrogen, air or another fluid less volatile than the medium-pressure nitrogen may possibly be condensed therein, provided that it condenses in another condenser of the system, normally above the reboiler. A portion of thestream 31 may serve as an oxygen-enriched product. - Next, the liquid containing 5 mol % nitrogen is sent to the low-pressure column at a level above the point of withdrawal of the
stream 26. - An
intermediate liquid 33 containing 80 mol % oxygen is sent from the mixing column to the low-pressure column 5. - The
bottom liquid 35 containing 65 mol % oxygen is sent from the mixing column to the low-pressure column 5. - A
stream 37 containing more than 99.5 mol % oxygen is withdrawn from the bottom of the low-pressure column 5 either in gaseous form or in liquid form. - It may thus be seen that the low-pressure column is fed, going from the top downwards, with lean liquid25 containing less than 1 mol % oxygen, with blowing
air 14, the unvaporized rich liquid 45 from the head condenser of the argon column, therich liquid 17, the liquid 35 from the bottom of the mixing column, the intermediate liquid 33 from the mixing column and therecondensed mixture 31 from the reboiler 7. - In order to further improve the arrangement, several intermediate liquids could be sent from the mixing column to the low-pressure column.
- The low-pressure column contains at least 80 theoretical trays and preferably at least 90 theoretical trays.
- The plant in FIG. 2 differs from that in FIG. 1 in that the mixing column is fed at the bottom exclusively with a stream of air possibly coming from a turbine or a supercharger (these not being illustrated). The vapour from the
condenser 21 of the argon column is sent to the low-pressure column just below the point of injection of therich liquid 45. - It would be conceivable to combine the concepts of FIGS. 1 and 2 and to feed the mixing column with air and with vaporized rich liquid at the same time.
- Obviously in the case of FIG. 2, the argon column may be omitted or reduced to a simple condenser fed by rich liquid and a gas from the low pressure column, for example having the composition of the feed to the argon column.
- As required, the argon column and/or the low-pressure column may be constructed in two sections in the manner described in EP-A-0628777.
- Likewise, the medium-pressure and low-pressure columns may be constructed side by side.
- These various staged feeds make it possible to obtain almost perfect low-pressure distillation. This allows the production of oxygen to be increased while maintaining, or even increasing, the production of argon when more than 10 to 15% of the air is withdrawn as medium-pressure nitrogen or 10 to 15% of the air is sent as blowing air.
- The refrigeration needed for the apparatus may be provided by a blowing turbine and/or a Claude turbine and/or a nitrogen turbine. The apparatus may produce liquids and/or gases.
Claims (29)
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9915208 | 1999-12-02 | ||
FR9915208A FR2801963B1 (en) | 1999-12-02 | 1999-12-02 | METHOD AND PLANT FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
Publications (2)
Publication Number | Publication Date |
---|---|
US20010003909A1 true US20010003909A1 (en) | 2001-06-21 |
US6385996B2 US6385996B2 (en) | 2002-05-14 |
Family
ID=9552807
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
US09/725,462 Expired - Fee Related US6385996B2 (en) | 1999-12-02 | 2000-11-30 | Process and installation for separation of air by cryogenic distillation |
Country Status (6)
Country | Link |
---|---|
US (1) | US6385996B2 (en) |
EP (1) | EP1106945B1 (en) |
JP (1) | JP2001194058A (en) |
AT (1) | ATE297001T1 (en) |
DE (1) | DE60020500T2 (en) |
FR (1) | FR2801963B1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2854232A1 (en) * | 2003-04-23 | 2004-10-29 | Air Liquide | Air separation procedure to produce argon uses cryogenic distillation with additional liquid flow containing 18-30 mol percent oxygen fed to low pressure column |
EP3557166A1 (en) | 2018-04-19 | 2019-10-23 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
Families Citing this family (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN102620520B (en) * | 2012-04-09 | 2014-09-17 | 开封黄河空分集团有限公司 | Process for preparing pressure oxygen and pressure nitrogen as well as by-product liquid argon through air separation |
CN103162512B (en) * | 2013-01-27 | 2015-06-10 | 南京瑞柯徕姆环保科技有限公司 | Air separation plant used for preparing oxygen and nitrogen in identical-pressure separation mode |
JP5655104B2 (en) | 2013-02-26 | 2015-01-14 | 大陽日酸株式会社 | Air separation method and air separation device |
Family Cites Families (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4022030A (en) | 1971-02-01 | 1977-05-10 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Thermal cycle for the compression of a fluid by the expansion of another fluid |
FR2584803B1 (en) * | 1985-07-15 | 1991-10-18 | Air Liquide | AIR DISTILLATION PROCESS AND INSTALLATION |
FR2655137B1 (en) * | 1989-11-28 | 1992-10-16 | Air Liquide | AIR DISTILLATION PROCESS AND INSTALLATION WITH ARGON PRODUCTION. |
FR2680114B1 (en) * | 1991-08-07 | 1994-08-05 | Lair Liquide | METHOD AND INSTALLATION FOR AIR DISTILLATION, AND APPLICATION TO THE GAS SUPPLY OF A STEEL. |
EP0636845B1 (en) * | 1993-04-30 | 1999-07-28 | The BOC Group plc | Air separation |
US5379599A (en) | 1993-08-23 | 1995-01-10 | The Boc Group, Inc. | Pumped liquid oxygen method and apparatus |
US5490391A (en) * | 1994-08-25 | 1996-02-13 | The Boc Group, Inc. | Method and apparatus for producing oxygen |
US5551258A (en) * | 1994-12-15 | 1996-09-03 | The Boc Group Plc | Air separation |
FR2774159B1 (en) * | 1998-01-23 | 2000-03-17 | Air Liquide | COMBINED INSTALLATION OF AN OVEN AND AN AIR DISTILLATION APPARATUS AND METHOD OF IMPLEMENTING IT |
US5865041A (en) * | 1998-05-01 | 1999-02-02 | Air Products And Chemicals, Inc. | Distillation process using a mixing column to produce at least two oxygen-rich gaseous streams having different oxygen purities |
GB9902101D0 (en) * | 1999-01-29 | 1999-03-24 | Boc Group Plc | Separation of air |
-
1999
- 1999-12-02 FR FR9915208A patent/FR2801963B1/en not_active Expired - Fee Related
-
2000
- 2000-11-30 US US09/725,462 patent/US6385996B2/en not_active Expired - Fee Related
- 2000-11-30 AT AT00403354T patent/ATE297001T1/en not_active IP Right Cessation
- 2000-11-30 EP EP00403354A patent/EP1106945B1/en not_active Expired - Lifetime
- 2000-11-30 DE DE60020500T patent/DE60020500T2/en not_active Expired - Fee Related
- 2000-12-04 JP JP2000368526A patent/JP2001194058A/en active Pending
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2854232A1 (en) * | 2003-04-23 | 2004-10-29 | Air Liquide | Air separation procedure to produce argon uses cryogenic distillation with additional liquid flow containing 18-30 mol percent oxygen fed to low pressure column |
EP3557166A1 (en) | 2018-04-19 | 2019-10-23 | Linde Aktiengesellschaft | Method for the low-temperature decomposition of air and air separation plant |
US11602713B2 (en) | 2018-04-19 | 2023-03-14 | Linde Aktiengesellschaft | Method for cryogenic separation of air, and air separation plant |
Also Published As
Publication number | Publication date |
---|---|
EP1106945A1 (en) | 2001-06-13 |
EP1106945B1 (en) | 2005-06-01 |
US6385996B2 (en) | 2002-05-14 |
FR2801963A1 (en) | 2001-06-08 |
JP2001194058A (en) | 2001-07-17 |
FR2801963B1 (en) | 2002-03-29 |
DE60020500D1 (en) | 2005-07-07 |
DE60020500T2 (en) | 2006-03-23 |
ATE297001T1 (en) | 2005-06-15 |
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