AU2009245592B2 - Method and apparatus for producing oxygen by separating air by cryogenic distillation - Google Patents
Method and apparatus for producing oxygen by separating air by cryogenic distillation Download PDFInfo
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- AU2009245592B2 AU2009245592B2 AU2009245592A AU2009245592A AU2009245592B2 AU 2009245592 B2 AU2009245592 B2 AU 2009245592B2 AU 2009245592 A AU2009245592 A AU 2009245592A AU 2009245592 A AU2009245592 A AU 2009245592A AU 2009245592 B2 AU2009245592 B2 AU 2009245592B2
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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
- F25J3/04151—Purification and (pre-)cooling of the feed air; recuperative heat-exchange with product streams
- F25J3/04163—Hot end purification of the feed air
- F25J3/04169—Hot end purification of the feed air by adsorption of the impurities
- F25J3/04181—Regenerating the adsorbents
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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
- F25J3/04048—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams
- F25J3/0406—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of cold gaseous streams, e.g. intermediate or oxygen enriched (waste) streams of nitrogen
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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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- 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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- F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
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- F25J3/04187—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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- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
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- 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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- 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
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- F25J3/04309—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 nitrogen
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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
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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
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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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- F25J3/04406—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
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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
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- 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
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- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- 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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Abstract
In a method for separating air by cryogenic distillation in an installation comprising a double column comprising a medium-pressure column (15) and a low-pressure column (17), the low-pressure column containing a bottom vaporizer (19), an intermediate vaporizer (21) and a top vaporizer (23), compressed air is purified in a purification unit, cooled in an exchange line and sent to the medium-pressure column of the double column, an oxygen-rich fluid is tapped from the low-pressure column, heated and sent to the client, nitrogen tapped from the medium-pressure column is split into at least three parts, a first part of the nitrogen is expanded in a first turbine (47), a second part of the nitrogen is compressed in a cold compressor (51) and sent to the bottom vaporizer, the nitrogen thus condensed being sent to at least one column of the double column, and a third part of the nitrogen is sent to the top vaporizer, without a pressure modifying step downstream of the column from which it is tapped and upstream of the top vaporizer, the nitrogen thus condensed being sent to at least one column of the double column, and a stream of gas is sent to the intermediate vaporizer, this stream consisting of compressed, purified and cooled air.
Description
1 Method and apparatus for separating air by cryogenic distillation The present invention relates to a method and to an apparatus for producing oxygen 5 by separating air using cryogenic distillation. It would be desirable to reduce the specific energy of separation of low-pressure low purity oxygen, particularly in schemes where the pressurized nitrogen is not realized as an asset in its own right by the end-customer. 10 The invention includes the use of a scheme employing three reboilers/condensers in the low-pressure column, in which: - the bottom reboiler/condenser operates on cold compressed medium pressure nitrogen 15 - the upper intermediate reboilers/condenser operates on 20 medium-pressure nitrogen - the lower intermediate reboilers/condenser operates either on medium pressure air or on medium-pressure nitrogen which is cold compressed. 20 Depending on variables, the specific energy saving represents between 0.5% and 7%. A reference herein to a patent document or other matter which is given as prior art is not to be taken as an admission that that document or matter was, in Australia, known 25 or that the information it contains was part of the common general knowledge as at the priority date of any of the claims. US-A-5006139 describes a method for producing nitrogen using a low-pressure column the bottom reboiler/condenser of which is heated by a flow of medium 30 pressure nitrogen compressed in a cold compressor. According to the invention, there is also a proposal to use several turbines in order better to optimize the exchange line.
WO 2009/136075 - 2 - PCT/FR2009/050617 The method of the present invention produces gaseous oxygen and preferably does not produce nitrogen from the medium-pressure column. 5 One subject of the invention provides a method for producing oxygen by separating air using cryogenic distillation in an installation comprising a double column comprising a medium-pressure and a low-pressure column, the low-pressure column containing a bottom 10 reboiler/condenser, an intermediate reboiler/condenser and an upper reboiler/condenser, in which method: a) compressed air is purified in a purification unit, cooled in an exchange line and fed to the medium pressure column of the double column 15 b) an oxygen-rich fluid is withdrawn from the low pressure column, heated up and sent to the customer c) nitrogen tapped off from the medium-pressure column is split into at least three parts d) a first part of the nitrogen is expanded in a 20 first turbine e) a second part of the nitrogen has its pressure raised in a cold compressor and is sent to the bottom reboiler/condenser, the nitrogen thus condensed being sent to at least one column of the double column 25 f) a third part of the nitrogen is sent to the upper reboiler/condenser, with no pressure-modifying step downstream of the column from which it is tapped off and upstream of the upper reboiler/condenser, the nitrogen thus condensed being sent to at least one 30 column of the double column g) a gaseous flow is sent to the intermediate reboiler/condenser, this flow consisting of purified and cooled compressed air or of the nitrogen tapped off from the medium-pressure column and compressed in a 35 cold compressor. According to other optional aspects: WO 2009/136075 - 3 - PCT/FR2009/050617 - the gaseous flow sent to the intermediate reboiler/condenser, is nitrogen from the medium pressure column - the gaseous flow sent to the intermediate 5 reboiler/condenser is purified and cooled compressed air - the first part of the nitrogen expanded in the first turbine is used for regenerating the purification unit 10 - the first turbine drives the cold compressor in which the pressure of the second part of the fluid is raised and provides substantially all the cold energy for the method - the low-pressure column has no top condenser 15 - all the gaseous nitrogen from the top of the medium-pressure column is split into just the three parts - all the gaseous nitrogen from the top of the medium-pressure column is split into just four parts, 20 the fourth part being sent to the intermediate reboiler/condenser - substantially all the cold energy is produced by expanding nitrogen from the medium-pressure column in at least one turbine 25 - a liquid oxygen flow from the low-pressure column is vaporized, possibly after pressurizing it, to produce the fluid sent to the customer. Another aspect of the invention provides an apparatus 30 for producing oxygen by separation of air using cryogenic distillation comprising a double column comprising a medium-pressure column and a low-pressure column, the low-pressure column containing a bottom reboiler/condenser, an intermediate reboiler/condenser 35 and an upper reboiler/condenser, a purification unit, an exchange line, at least one first turbine, at least one cold compressor, means for sending compressed air, WO 2009/136075 - 4 - PCT/FR2009/050617 purified in the purification unit and cooled in the exchange line, to the medium-pressure column of the double column, means for withdrawing an oxygen-rich fluid from the low-pressure column, means for possibly 5 heating it up, said means consisting at least in part of the exchange line and means for sending the heated up oxygen-rich fluid sent to the customer, means for splitting the nitrogen tapped off from the medium pressure column into at least three parts, means for 10 sending a first part of the nitrogen to a first turbine, means for sending a second part of the nitrogen to a cold compressor where its pressure can be raised, means for sending the raised-pressure second part to the bottom reboiler/condenser, means for 15 sending the nitrogen thus condensed to at least one column of the double column, means for sending a third part of the nitrogen to the upper reboiler/condenser, without a pressure modifying means downstream of the column from which it was tapped off and upstream of the 20 upper reboiler/condenser, means for sending the nitrogen thus condensed being sent to at least one column of the double column, means for sending a gaseous flow to the intermediate reboiler/condenser, this flow consisting of purified and cooled compressed 25 air or of nitrogen tapped off from the medium-pressure column and compressed in the second cold compressor. The apparatus may possibly comprise: - means for connecting the intermediate 30 reboiler/condenser to the top of the medium-pressure column - means for connecting the outlet of the first turbine to the purification unit - the first turbine is coupled to the cold 35 compressor in which the pressure of the second part of the fluid is raised and constitutes the only turbine in the apparatus WO 2009/136075 - 5 - PCT/FR2009/050617 - the low-pressure column has no top condenser - means for vaporizing liquid oxygen, possibly in the exchange line, and possibly means for pressurizing liquid oxygen upstream of the means for vaporizing the 5 liquid oxygen. The invention will be described in greater detail with reference to figures 1, 2 and 3 which are schematic diagrams of air separation apparatuses according to the 10 invention. Figure 1 shows an air separation apparatus in which a pressurized and purified air flow 1 is split into three flows 3, 5, 7. The flow 3 is cooled as it passes from 15 one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column. The flow 5 is cooled as it passes from one end of the exchange line 11 to the other and is sent to an intermediate reboiler/condenser 21 of the low-pressure 20 column 17 of the double column 15, 17. The other air flow 7 has its pressure raised in a hot pressurizer 9, is cooled by passing from one end of the exchange line 11 to the other and is sent to a reboiler/condenser 13 where it condenses at least partially by exchanging 25 heat with pressurized liquid oxygen. The condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17. 30 Rich liquid 25, lean liquid 61 and possibly a liquid 27 somewhat like liquid air are sent from the medium pressure column 15 to the low-pressure column 17 as reflux flows after supercooling in the exchanger 29. 35 A flow of liquid oxygen 33 is tapped off from the low pressure column, pressurized by the pump 35 and vaporized in the reboiler/condenser 13 upstream of the WO 2009/136075 - 6 - PCT/FR2009/050617 exchange line 11. The fluid 33 may also be compressed by the effect of a hydrostatic head, without the pump 35. 5 Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and is heated up in the exchangers 29, 11. A medium-pressure gaseous flow of nitrogen 39 is tapped 10 off from the top of the medium-pressure column 15 and split into two.. One part 53 is sent to. an upper reboiler/condenser 23 of the low-pressure column 17 where it condenses before being returned to the medium pressure column by way of reflux. The remainder of the 15 nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55, and this flow 55 is sent to the bottom reboiler/condenser 19 of the low-pressure column 17. In this reboiler/condenser 19 it condenses and then acts as 20 reflux for at least one of the columns. The remainder 45 of the nitrogen is sent to the exchange line, is heated up to an intermediate level, and is sent to a turbine 47. The nitrogen expanded in 25 the turbine 47 is sent to the cold end of the exchange line and heats up, becoming the flow 49. This yields a potential energy saving of 0.5% over the scheme disclosed in WO-A-2007/129152. 30 Figure 2 shows an air separation apparatus in which a pressurized and purified air flow 1 is split into two flows 3,7. The flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to 35 the medium-pressure column 15 of a double column. The other air flow 7 has its pressure raised in a hot pressurizer 9, is cooled as it passes from one end of WO 2009/136075 - 7 - PCT/FR2009/050617 the exchange line 11 to the other and is sent to a reboiler/condenser 13 where it condenses at least in part by exchange of heat with pressurized liquid oxygen. The condensed air is either sent in its 5 entirety to the medium-pressure column or split between the medium-pressure column and the low-pressure column 17. Rich liquid 25, lean liquid 61 and possibly a liquid 27 10 somewhat like liquid air are sent from the medium pressure column 15 to the low-pressure column 17 as reflux flows after supercooling in the exchanger 29. A flow of liquid oxygen 33 is tapped off from the low 15 pressure column, pressurized by the pump 35 and vaporized in the reboiler/condenser 13 upstream of the exchange line 11. The fluid 33 may also be compressed using a hydrostatic head, without the pump 35. 20 Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and heats up in the exchangers 29, 11. A medium-pressure gaseous flow of nitrogen 39 is tapped 25 off from the top of the medium-pressure column 15 and split into two. One part 53 is sent to an upper reboiler/condenser 23 of the low-pressure column 17 where it condenses before being returned to the medium pressure column by way of reflux. The remainder of the 30 air is once again split into two. One fraction is sent to the cold compressor 151 to become the flow 155 which heats the intermediate reboiler/condenser 21 before being sent to the columns by way of reflux. The remainder of the nitrogen 41 is split into two, one 35 portion 43 being sent to a cold compressor 51 to form a flow 55, and this flow 55 is sent to the bottom reboiler/condenser 19 of the low-pressure column 17. In WO 2009/136075 - 8 - PCT/FR2009/050617 this reboiler/condenser 19 it condenses and then serves as reflux for at least one of the columns. The remainder 45 of the nitrogen is sent to the 5 exchange line, is heated up to an intermediate level and is sent to a turbine 47. The nitrogen expanded in the turbine 47 is sent to the cold end of the exchange line and heats up, becoming the flow 49. Having the two cold compressors 51, 151 on the medium-pressure 10 nitrogen line allows the distribution of power across the compressors to be adjusted to best suit the low pressure column reboiling requirement. An energy saving of 1.7% over the scheme of 15 WO-A-2007/129152 can be achieved. Figure 3 shows an air separation apparatus in which an air flow 1, pressurized by a compressor M and purified in a purification unit 2 is split into two flows 3, 7. 20 The flow 3 is cooled as it passes from one end of the exchange line 11 to the other and is sent to the medium-pressure column 15 of a double column. The other 7 has its pressure raised in a hot pressurizer 9, is cooled by passing from one end of the exchange line 11 25 to the other and is sent to a reboiler/condenser 13 where it condenses at least in part by exchange of heat with pressurized liquid oxygen. The condensed air is either sent in its entirety to the medium-pressure column or split between the medium-pressure column and 30 the low-pressure column 17. Rich liquid 25, lean liquid 61, and possibly a liquid 27 somewhat like liquid air are sent from the medium pressure column 15 to the low-pressure column 17 by way 35 of reflux flows following supercooling in the exchanger 29.
WO 2009/136075 - 9 - PCT/FR2009/050617 A flow of liquid oxygen 33 is tapped off from the low pressure column, pressurized by the pump 35 and vaporized in the reboiler/condenser 13 upstream of the exchange line 11. The fluid 33 may also be compressed 5 using a hydrostatic head, without the pump 35. Low-pressure nitrogen 31 is tapped off from the top of the low-pressure column 17 and is heated up in the exchangers 29, 11. 10 A medium-pressure gaseous flow of nitrogen 39 is tapped off from the top of the medium-pressure column 15 and split into two. One part 53 is sent to an upper reboiler/condenser 23 of the low-pressure column 17 15 where it condenses before being returned to the medium pressure column by way of reflux. The remainder of the air is once again split into two. One fraction is sent to the cold compressor 151 where it becomes the flow 155, the flow 155 being cooled in the exchange line 11 20 before being used to heat the intermediate reboiler/condenser 21 before being sent to the columns by way of reflux. The remainder of the nitrogen 41 is split into two, one portion 43 being sent to a cold compressor 51 to form a flow 55, and this flow 55 is 25 sent to the bottom reboiler/condenser 19 of the low pressure column 17 after having been cooled in the exchange line 11. In this reboiler/condenser 19 it condenses and then serves as reflux for at least one of the columns. 30 The remainder 45 of the nitrogen is sent to the exchange line, heats up to an intermediate level and is split into two. One part 49 of the nitrogen 45 is sent to a turbine 47. The nitrogen expanded in the turbine 35 47 is sent to the cold end of the exchange line and is heated up before being used periodically to regenerate the purification unit 2. The remainder of the nitrogen 9A 46 continues to be heated up in the exchange line 11 and is split into two, one part 149 being sent to a turbine 147 at a higher inlet temperature than the turbine 47. This part of the nitrogen is expanded, heated up and discharged into the atmosphere. The remainder 249 of the nitrogen is sent to a turbine 247 at a higher inlet temperature 5 than the turbines 47, 147. This part 249 of the nitrogen is expanded, heated up and discharged into the atmosphere. An energy saving of 7% over the scheme of WO-A-2007/129152 can be achieved. 10 Throughout the description and claims of this specification the word "comprise" and variations of that word, such as "comprises" and "comprising", are not intended to exclude other additives or components or integers. C-\nnf\word\SPFC.RQ7.77 dn-'v
Claims (12)
1. A method for producing oxygen by separating air using cryogenic distillation in an installation comprising a double column comprising a medium-pressure column 5 and a low-pressure column, the low-pressure column containing the bottom reboiler/condenser, an intermediate reboiler/condenser and an upper reboiler/condenser, in which method: a) compressed air is purified in a purification unit, cooled in an exchange line and fed to the medium-pressure column of the double column 10 b) an oxygen-rich fluid is withdrawn from the low-pressure column, heated up and sent to the customer c) nitrogen tapped off from the medium-pressure column is split into at least three parts d) a first part of the nitrogen is expanded in a first turbine 15 e) a second part of the nitrogen has its pressure raised in a cold compressor and is sent to the bottom reboiler/condenser, the nitrogen thus condensed being sent to at least one column of the double column f) a third part of the nitrogen is sent to the upper reboiler/coridenser, with no pressure-modifying step downstream of the column from which it is tapped off and 20 upstream of the upper reboiler/condenser, the nitrogen thus condensed being sent to at least one column of the double column g) a gaseous flow is sent to the intermediate reboiler/condenser, this flow consisting of the nitrogen tapped off from the medium-pressure column and compressed in a cold compressor. 25
2. The method as claimed in any one of the preceding claims, in which the first part of the nitrogen expanded in the first turbine is used for regenerating the purification unit. 30
3. The method as claimed in either of the preceding claims, in which the first turbine drives the cold compressor in which the pressure of the second part of the nitrogen is raised and provides substantially all the cold energy for the method. C:\of\worSPFC-R97127 dnn 11
4. The method as claimed in any one of the preceding claims, in which the low pressure column has no top condenser.
5. The method as claimed in any one of the preceding claims, in which all the 5 gaseous nitrogen from the top of the medium-pressure column is split into just the three parts.
6. The method as claimed in any one of claims 1 to 4, in which all the gaseous nitrogen from the top of the medium-pressure column is split into just four parts, the 10 fourth part being sent to the intermediate reboiler/condenser.
7. The method as claimed in any one of the preceding claims, in which substantially all the cold energy is produced by expanding nitrogen from the medium pressure column in at least one turbine. 15
8. The method as claimed in any one of the preceding claims, in which a liquid oxygen flow from the low-pressure column is vaporized, possibly after pressurizing it, to produce the fluid sent to the customer. 20
9. An apparatus for producing oxygen by separation of air using cryogenic distillation comprising a double column comprising a medium-pressure column and a low-pressure column, the low-pressure column containing a bottom reboiler/condenser, an intermediate reboiler/condenser and an upper reboiler/condenser, a purification unit, an exchange line, at least one first turbine, at 25 least one cold compressor, means for sending compressed air, purified in the purification unit and cooled in the exchange line, to the medium-pressure column of the double column, means for withdrawing an oxygen-rich fluid from the low-pressure column, means for possibly heating it up, said means consisting at least in part of the exchange line and means for sending the heated-up oxygen-rich fluid sent to the 30 customer, means for splitting the nitrogen tapped off from the medium-pressure column into at least three parts, means for sending a first part of the nitrogen to the first turbine, means for sending a second part of the nitrogen to the cold compressor where its pressure can be raised, means for sending the raised-pressure second part to the bottom reboiler/condenser, means for sending the nitrogen thus condensed to 12 at least one column of the double column, means for sending a third part of the nitrogen to the upper reboiler/condenser, without a pressure modifying means downstream of the column from which it was tapped off and upstream of the upper reboiler/condenser, means for sending the nitrogen thus condensed being sent to at 5 least one column of the double column, means for sending a gaseous flow to the intermediate reboiler/condenser, this flow consisting of purified and cooled compressed air or of nitrogen tapped off from the medium-pressure column and compressed in the second cold compressor, wherein it comprises means for connecting the intermediate reboiler/condenser to the top of the medium-pressure 10 column so that the nitrogen tapped off from the top of this column is sent to the intermediate reboiler/condenser.
10. The apparatus as claimed in claim 9, comprising means for connecting the outlet of the first turbine to the purification unit. 15
11. The apparatus as claimed in either of claims 9 and 10, in which the first turbine is coupled to the cold compressor in which the pressure of the second part of the fluid is raised and constitutes the only turbine in the apparatus. 20
12. The apparatus as claimed in any one of claims 9 to 11, in which the low pressure column has no top condenser.
Applications Claiming Priority (13)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0852706A FR2930327A1 (en) | 2008-04-22 | 2008-04-22 | Air separating method for carbon oxycombustion frame, involves sending oxygen and nitrogen enrich liquids, and reheating nitrogen rich flow from low pressure columns and oxygen rich flow in exchange line |
FR0852710A FR2930331B1 (en) | 2008-04-22 | 2008-04-22 | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
FR0852709 | 2008-04-22 | ||
FR0852708A FR2930329A1 (en) | 2008-04-22 | 2008-04-22 | Air separating method, involves sending residual oxygen directly to atmosphere through tower in direct contact with water at hot end of exchange line and cold compressor that uses part of refrigerated power of turbine |
FR0852705A FR2930326B1 (en) | 2008-04-22 | 2008-04-22 | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
FR0852705 | 2008-04-22 | ||
FR0852707 | 2008-04-22 | ||
FR0852709A FR2930330B1 (en) | 2008-04-22 | 2008-04-22 | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
FR0852708 | 2008-04-22 | ||
FR0852706 | 2008-04-22 | ||
FR0852707A FR2930328A1 (en) | 2008-04-22 | 2008-04-22 | Air separating method for oxycombustion application in boiler, involves sending oxygen and nitrogen enriched liquids to low pressure column, removing oxygen enriched gas in condenser, and drawing nitrogen enriched gas from column |
FR0852710 | 2008-04-22 | ||
PCT/FR2009/050617 WO2009136075A2 (en) | 2008-04-22 | 2009-04-08 | Method and apparatus for separating air by cryogenic distillation |
Publications (2)
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AU2009245592A1 AU2009245592A1 (en) | 2009-11-12 |
AU2009245592B2 true AU2009245592B2 (en) | 2013-09-19 |
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Application Number | Title | Priority Date | Filing Date |
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AU2009245592A Ceased AU2009245592B2 (en) | 2008-04-22 | 2009-04-08 | Method and apparatus for producing oxygen by separating air by cryogenic distillation |
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US (1) | US20110067445A1 (en) |
EP (1) | EP2268990A2 (en) |
JP (1) | JP2011518307A (en) |
CN (1) | CN102016469A (en) |
AU (1) | AU2009245592B2 (en) |
CA (1) | CA2722261A1 (en) |
FR (1) | FR2930330B1 (en) |
WO (1) | WO2009136075A2 (en) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
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FR2930331B1 (en) * | 2008-04-22 | 2013-09-13 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
FR2973865B1 (en) * | 2011-04-08 | 2015-11-06 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
US9097459B2 (en) | 2011-08-17 | 2015-08-04 | Air Liquide Process & Construction, Inc. | Production of high-pressure gaseous nitrogen |
US20130042647A1 (en) * | 2011-08-18 | 2013-02-21 | Air Liquide Process & Construction, Inc. | Production Of High-Pressure Gaseous Nitrogen |
EP2758734B1 (en) * | 2011-09-20 | 2018-07-18 | Linde Aktiengesellschaft | Method and device for cryogenic decomposition of air |
FR2990500A1 (en) * | 2012-05-11 | 2013-11-15 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
EP3019803B1 (en) * | 2013-07-11 | 2022-04-20 | Linde GmbH | Method and device for oxygen production by low-temperature separation of air at variable energy consumption |
FR3011916B1 (en) * | 2013-10-15 | 2015-11-13 | Air Liquide | METHOD AND APPARATUS FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
US10101084B2 (en) * | 2015-07-31 | 2018-10-16 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Apparatus for the production of low pressure gaseous oxygen |
US10018414B2 (en) * | 2015-07-31 | 2018-07-10 | L'air Liquide Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method for the production of low pressure gaseous oxygen |
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2008
- 2008-04-22 FR FR0852709A patent/FR2930330B1/en active Active
-
2009
- 2009-04-08 CN CN2009801143457A patent/CN102016469A/en active Pending
- 2009-04-08 AU AU2009245592A patent/AU2009245592B2/en not_active Ceased
- 2009-04-08 JP JP2011505563A patent/JP2011518307A/en active Pending
- 2009-04-08 CA CA2722261A patent/CA2722261A1/en not_active Abandoned
- 2009-04-08 US US12/937,608 patent/US20110067445A1/en not_active Abandoned
- 2009-04-08 WO PCT/FR2009/050617 patent/WO2009136075A2/en active Application Filing
- 2009-04-08 EP EP09742273A patent/EP2268990A2/en not_active Withdrawn
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Also Published As
Publication number | Publication date |
---|---|
EP2268990A2 (en) | 2011-01-05 |
WO2009136075A3 (en) | 2010-10-07 |
AU2009245592A1 (en) | 2009-11-12 |
WO2009136075A4 (en) | 2010-11-25 |
CN102016469A (en) | 2011-04-13 |
US20110067445A1 (en) | 2011-03-24 |
FR2930330A1 (en) | 2009-10-23 |
FR2930330B1 (en) | 2013-09-13 |
JP2011518307A (en) | 2011-06-23 |
CA2722261A1 (en) | 2009-11-12 |
WO2009136075A2 (en) | 2009-11-12 |
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