WO2010109149A2 - Apparatus and method for separating air by cryogenic distillation - Google Patents
Apparatus and method for separating air by cryogenic distillation Download PDFInfo
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- WO2010109149A2 WO2010109149A2 PCT/FR2010/050550 FR2010050550W WO2010109149A2 WO 2010109149 A2 WO2010109149 A2 WO 2010109149A2 FR 2010050550 W FR2010050550 W FR 2010050550W WO 2010109149 A2 WO2010109149 A2 WO 2010109149A2
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04769—Operation, control and regulation of the process; Instrumentation within the process
- F25J3/04854—Safety aspects of operation
- F25J3/0486—Safety aspects of operation of vaporisers for oxygen enriched liquids, e.g. purging of liquids
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D25/00—Pumping installations or systems
- F04D25/02—Units comprising pumps and their driving means
- F04D25/04—Units comprising pumps and their driving means the pump being fluid-driven
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F04—POSITIVE - DISPLACEMENT MACHINES FOR LIQUIDS; PUMPS FOR LIQUIDS OR ELASTIC FLUIDS
- F04D—NON-POSITIVE-DISPLACEMENT PUMPS
- F04D25/00—Pumping installations or systems
- F04D25/02—Units comprising pumps and their driving means
- F04D25/06—Units comprising pumps and their driving means the pump being electrically driven
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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
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- 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
- F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
- F25J3/04024—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of purified feed air, so-called boosted air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
- F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04115—Arrangements of compressors and /or their drivers characterised by the type of prime driver, e.g. hot gas expander
- F25J3/04133—Electrical motor as the prime mechanical driver
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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
- F25J3/04109—Arrangements of compressors and /or their drivers
- F25J3/04145—Mechanically coupling of different compressors of the air fractionation process to the same driver(s)
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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
- F25J3/04187—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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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
- F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
- F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
- F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
- F25J3/04418—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system with thermally overlapping high and low pressure columns
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04763—Start-up or control of the process; Details of the apparatus used
- F25J3/04866—Construction and layout of air fractionation equipments, e.g. valves, machines
- F25J3/04872—Vertical layout of cold equipments within in the cold box, e.g. columns, heat exchangers etc.
- F25J3/04878—Side by side arrangement of multiple vessels in a main column system, wherein the vessels are normally mounted one upon the other or forming different sections of the same 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
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/40—One fluid being air
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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2250/00—Details related to the use of reboiler-condensers
- F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
- F25J2250/50—One fluid being oxygen
Definitions
- the present invention relates to an apparatus and method for air separation by air distillation. It is known from Ramsdohr's Optimize air compressor performance for GTL Plants, Hydrocarbon Processing, January 2004 to use an axial-radial type compressor as the main air compressor (MAC) of a separation apparatus. air compressing all the air intended for distillation. These compressors can compress air flow rates higher than centrifugal compressors (single shaft or transmission which are limited to -500 000 m3 / h maximum).
- the air booster called BAC compresses only a portion of the air and is constituted by a centrifugal compressor.
- axial-radial type compressors combine in the same machine an axial portion (whose compression ratio is typically ⁇ 3) and a radial portion consisting of 1 to 3 wheels.
- the fins of the axial portion and the wheels of the radial portion are installed on the same shaft.
- a refrigerant is installed between the axial and radial parts. All the flow of the axial part passes in the radial part (with the losses near).
- WO-A-2009/007310 discloses a compression method using a first machine which is a radial compressor and a second machine which is a radial compressor, the two machines being driven by the same drive means.
- an air separation installation comprising a column system comprising at least one medium pressure column and at least one low pressure column, possibly thermally connected to each other, a main exchanger, a compressor of main air, means for producing gaseous oxygen at a pressure of less than 5 bar abs, comprising means for withdrawing an oxygen-enriched liquid flow from the column system and for sending it vaporization means constituted by the main exchanger or independent vaporizer of the main exchanger, means for heating the oxygen-rich gas produced by the vaporization of the oxygen enriched liquid, these heating means being constituted by the main exchanger, means for sending all the air to be treated in the system of columns at a first axial portion of the main compressor for producing air at the pressure P1 of the medium pressure column, means for sending a first portion of the air substantially at the pressure of the medium pressure column to the middle column pressure, means for sending a second portion of the air substantially to the pressure of the medium pressure column to a second radial or centrifugal portion of the main compressor to bring it
- the installation includes:
- the first part and the second part of the compressor are each provided with guide vanes;
- the second part of the compressor comprises a first section and a second section, means for sending all the second part of the air substantially at medium pressure to the first section to pressurize it at the high pressure, means for dividing the second section; part of the air in two to form a first flow and a second flow, means for sending the first flow to the main exchanger and possibly to the vaporizer, means for sending the second flow to the second section to pressurize it to a high pressure higher than the high pressure and means for sending the second flow at the high pressure to the main exchanger and then to a vaporizer of the low pressure column, preferably a tank vaporizer of the low pressure column.
- an air separation method producing oxygen gas at a pressure of less than 5 bar abs, using a column system comprising at least one medium-pressure column and at least one low pressure column, a main exchanger, a main compressor having stages in which: a) the totality Q1 of the treated air is compressed to a first pressure P1 which corresponds to the pressure of the medium pressure column, to the losses of charge near b) a portion Q2 of this air at the pressure P1 is supercharged to a high pressure P2, greater than P1, which allows the vaporization of liquid oxygen in the main exchanger or in a dedicated vaporizer by heat exchange with a flow of liquid oxygen c) the flow of liquid oxygen is withdrawn from the low pressure column, possibly pressurized at a pressure of less than 5 bar abs, and sent to the main exchanger 1 or to a dedicated vaporizer where it vaporizes by heat exchange with at least the part of the air at the high pressure P2 d) the totality Q1 of the air is compressed in
- the pressure P1 is less than 4.5 bar abs, preferably less than 4 bar, even less than 3.5 bar abs;
- the pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs; the flow rate of Q2 compressed to the pressure P2 is less than half the flow rate of Q1, and preferably less than one third of the flow rate of Q1;
- the second part of the main compressor comprises a first section and a second section and in which the whole part Q2 of the air is compressed to the pressure P2 in the first section, the part Q2 is divided in two to form a first section; and a second flow rate, the first flow rate being cooled in the main exchanger and optionally sent to the vaporizer at the high pressure P2 and the second flow rate being supercharged to a high pressure P3, higher than the pressure P2, cooled to the high pressure in the main exchanger and used to heat a vaporizer of the low pressure column, preferably the vessel vaporizer;
- a part of the air at the first pressure P1 is sent to an intermediate vaporizer of the low pressure column where it condenses, the condensed air being sent to the medium pressure column; the whole Q1 of the compressed compressed air is dried up to a first pressure P1 in the first part of the compressor.
- the apparatus comprises an exchange line 21 and a double column constituted by a medium pressure column 27 and a low pressure column 29.
- All the air 1 is compressed in the first part 3 of a main compressor 4 constituted by at least one axial stage to produce air at the pressure P1 substantially equal to the pressure of the medium pressure column 27.
- the first part preferably comprises several stages, all axial.
- the air at pressure P1 is cooled in a cooler 7 (which can be either a tubular exchanger or a tower air / water one or two stages), purified in a purification unit 9 and divided into three fractions.
- the first fraction 11 is supercharged in at least the last stage of the main compressor, the last stage which is part of the second part of the compressor. This last stage and preferably all the stages of the second part are radial stages or centrifugal stages.
- the main compressor with its first part and its second is a single machine with a single frame and the first part and the second part of the compressor are driven by the same way, in the example an engine M.
- the pressure P1 is less than 5 bar abs, or even 4.5 bar abs, preferably less than 4 bar, and still less than 3.5 bar abs
- the first fraction 11 is fed by the second part 5 of the main compressor to a pressure P2 and cools to this pressure in the exchange line 21.
- the fraction 11 is then sent to a vaporizer 41 where it condenses at least partially before to be relaxed and sent to the medium pressure column 27.
- the pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs.
- Fraction 11 is less than half of flow 1, and preferentially less than one third of flow 1
- the second fraction 13 at the pressure P1 cools completely in the exchange line 21 and is divided into two streams.
- the first stream 23 is sent to a bottom reboiler 33 of the low pressure column 29 where it condenses at least partially and is sent to the medium pressure column, mixed with the flow rate 11.
- the second stream 25 is sent in gaseous form to the medium pressure column 27.
- the third fraction 15 is supercharged in a booster 17 driven by a cryogenic turbine 19, partially cooled in the exchange line 21, withdrawn from the exchange line at an intermediate level thereof and expanded in the turbine 19 before to be sent to the low pressure column
- An oxygen-enriched liquid flow 55, an intermediate flow 53 and a nitrogen-rich liquid flow 51 are withdrawn from the medium-pressure column 27, cooled in the exchanger 31, expanded and sent to different levels of the low-pressure column 29 .
- Medium pressure nitrogen gas 49 is condensed in an intermediate vaporizer 35 of the low pressure column 29 and sent as reflux to the top of the medium pressure column 27. Another flow of medium pressure nitrogen gas 47 is heated in the line of 'exchange.
- Liquid oxygen 37 is withdrawn in the bottom of the low pressure column 29, pressurized by a pump 39 at a pressure lower than 5 bar abs and sent to the vaporizer 41. Apart from a liquid purge 43, the oxygen vaporizes in the vaporizer 41 by heat exchange with the air fraction 11 to the P2 pressure. The oxygen then forms the flow rate of pressurized gaseous oxygen 45 which heats up in the exchange line 21.
- the apparatus comprises an exchange line 21 and a double column formed by a medium pressure column 27 and a low pressure column 29.
- the low pressure column differs from that of FIG. three vaporizers 33, 34.35 instead of two.
- All the air 1 is compressed in the first part 3 of a main compressor 4 constituted by at least one axial stage to produce air at the pressure P1 substantially equal to the pressure of the medium pressure column 27.
- the first part preferably comprises several stages, all axial.
- the air at pressure P1 is cooled in a cooler 7, purified in a purification unit 9 and divided into three fractions.
- the first fraction 11 is supercharged in the first section 5A of the second part of the main compressor 4.
- the first section 5A is preferably composed entirely of radial or centrifugal stages.
- the main compressor with its first part and its second part, in two sections, is a single machine with a single frame and the first part and the second part of the compressor are driven by the same means, in the example an engine M.
- the pressure P1 is less than 5 bar abs, even 4.5 bar abs, preferably less than 4 bar, and still less than 3.5 bar abs
- the first fraction 11 is fed through the first section 5A of the second part of the main compressor at a high pressure P2 and divides into two flow rates.
- the first flow 26 cools at this pressure P2 in the exchange line 21.
- the first flow 26 is then sent to a vaporizer 41 where it condenses at least partially before being expanded and sent to the medium pressure column 27.
- the pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs.
- the first fraction 11 is less than half the flow 1, and preferably less than one-third of the flow 1.
- the second flow 23 is supercharged at a high pressure P3 in the second section 5B of the second part of the compressor 4.
- the second section 5B is composed, preferably entirely, of the same type of stages as the first section 5A, whether it is radial or centrifugal stages.
- the flow 23 at the high pressure cools in the main exchanger 21 and is sent to the vaporizer 33 in the tank of the low pressure column 29. It is also possible to send this flow to one of the upper vaporizer 34,35. There the flow 23 condenses at least partially and is sent to be mixed with the flow 26 condensed in the vaporizer 41.
- the second fraction 13 at the pressure P1 cools completely in the exchange line 21 and is divided into two streams.
- the first stream 24 is sent to an intermediate vaporizer 34 of the low pressure column 29 where it condenses at least partially and is sent to the medium pressure column, mixed with the flow rate 26.
- the second stream 25 is sent in gaseous form to the column medium pressure 27.
- the third fraction 15 is supercharged in a booster 17 driven by a cryogenic turbine 19, partially cooled in the exchange line 21, withdrawn from the exchange line at an intermediate level thereof and expanded in the turbine 19 before to be sent to the low pressure column 29.
- An oxygen-enriched liquid flow 55, an intermediate flow 53 and a nitrogen-rich liquid flow 51 are withdrawn from the medium-pressure column 27, cooled in the exchanger 31, expanded and sent to different levels of the low-pressure column 29
- Medium pressure nitrogen gas 49 is condensed in an upper vaporizer 35 of the low pressure column 29 and sent as reflux to the top of the medium pressure column 27.
- Liquid oxygen 37 is withdrawn in the bottom of the low pressure column 29, pressurized by a pump 39 at a pressure lower than 5 bar abs and sent to the vaporizer 41. Apart from a liquid purge 43, the oxygen vaporizes in the vaporizer 41 by heat exchange with the air flow 26 at the pressure P2. The oxygen then forms the rate of pressurized oxygen gas 45 which heats up in the exchange line 21, which is the main product of the apparatus. While the preceding figures illustrate double columns, it is conceivable to split the low pressure column into two or even three (as in Figure 2) to reduce the height of columns. Similarly the medium pressure column can be placed next to the low pressure column (s).
- the compressor can be controlled by guide vanes which are provided with the first and second part. Otherwise a rolling valve can be placed at the inlet of the second part of the compressor, to control the second part of the compressor.
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Abstract
Description
Appareil et procédé de séparation d'air par distillation cryogénique Apparatus and method for separating air by cryogenic distillation
La présente invention est relative à un appareil et procédé de séparation d'air par distillation d'air. II est connu de « Optimize air compressor performance for GTL Plants » de Ramsdohr, Hydrocarbon Processing, janvier 2004 d'utiliser un compresseur de type axial-radial en tant que compresseur d'air principal (MAC) d'un appareil de séparation d'air comprimant tout l'air destiné à la distillation. Ces compresseurs permettent de comprimer des débits d'air supérieurs à ceux des compresseurs centrifuges (à arbre unique ou à transmission qui sont limités à -500 000 m3/h maximum). Le surpresseur d'air dénommé BAC ne comprime qu'une partie de l'air et est constitué par un compresseur centrifuge.The present invention relates to an apparatus and method for air separation by air distillation. It is known from Ramsdohr's Optimize air compressor performance for GTL Plants, Hydrocarbon Processing, January 2004 to use an axial-radial type compressor as the main air compressor (MAC) of a separation apparatus. air compressing all the air intended for distillation. These compressors can compress air flow rates higher than centrifugal compressors (single shaft or transmission which are limited to -500 000 m3 / h maximum). The air booster called BAC compresses only a portion of the air and is constituted by a centrifugal compressor.
Ces compresseurs de type axial-radial combinent dans une même machine une partie axiale (dont le taux de compression est typiquement de ~3) et une partie radiale constituée de 1 à 3 roues. Les ailettes de la partie axiale et les roues de la partie radiale sont installées sur un même arbre. Un réfrigérant est installé entre les parties axiales et radiales. Tout le débit de la partie axiale passe dans la partie radiale (aux pertes près).These axial-radial type compressors combine in the same machine an axial portion (whose compression ratio is typically ~ 3) and a radial portion consisting of 1 to 3 wheels. The fins of the axial portion and the wheels of the radial portion are installed on the same shaft. A refrigerant is installed between the axial and radial parts. All the flow of the axial part passes in the radial part (with the losses near).
Il est également connu de combiner dans des machines de type multi- intégrées un MAC et un BAC : sur un même multiplicateur, et dans un même bâti (en anglais « casing »), on installe des pignons pour le MAC et des pignons pour le BAC. Des exemples se trouvent dans EP-A-0689019 et EP-A-0877217.It is also known to combine in multi-integrated type machines a MAC and a BAC: on the same multiplier, and in the same frame (in English "casing"), one installs gables for the MAC and gears for the BAC. Examples are in EP-A-0689019 and EP-A-0877217.
WO-A-2009/007310 décrit un procédé de compression utilisant une première machine qui est un compresseur radial et une deuxième machine qui est un compresseur radial, les deux machines étant entraînées par le même moyen d'entraînement.WO-A-2009/007310 discloses a compression method using a first machine which is a radial compressor and a second machine which is a radial compressor, the two machines being driven by the same drive means.
Selon un objet de l'invention, il est prévu une installation de séparation d'air comprenant système de colonnes comprenant au moins une colonne moyenne pression et au moins une colonne basse pression, éventuellement thermiquement reliées entre elles, un échangeur principal, un compresseur d'air principal, des moyens pour produire de l'oxygène gazeux à une pression inférieure à 5 bar abs, comprenant des moyens pour soutirer un débit liquide enrichi en oxygène du système de colonnes et pour l'envoyer des moyens de vaporisation constitués par l'échangeur principal ou un vaporiseur indépendant de l'échangeur principal, des moyens de réchauffage du gaz riche en oxygène produit par la vaporisation du liquide enrichi en oxygène, ces moyens de réchauffage étant constitués par l'échangeur principal, des moyens pour envoyer tout l'air à traiter dans le système de colonnes à une première partie axiale du compresseur principal pour produire de l'air à la pression P1 de la colonne moyenne pression, des moyens pour envoyer une première partie de l'air substantiellement à la pression de la colonne moyenne pression à la colonne moyenne pression, des moyens pour envoyer une deuxième partie de l'air substantiellement à la pression de la colonne moyenne pression à une deuxième partie radiale ou centrifuge du compresseur principal pour l'amener au moins jusqu'à une pression élevée P2, des moyens pour envoyer l'air à la pression élevée provenant de la deuxième partie à l'échangeur principal et éventuellement ensuite au vaporiseur, la première partie et la deuxième partie du compresseur étant sur un même arbre, dans un même bâti, et entraînées par un même moyen d'entraînement, tel qu'un moteur électrique ou une ou plusieurs turbine(s).According to one object of the invention, there is provided an air separation installation comprising a column system comprising at least one medium pressure column and at least one low pressure column, possibly thermally connected to each other, a main exchanger, a compressor of main air, means for producing gaseous oxygen at a pressure of less than 5 bar abs, comprising means for withdrawing an oxygen-enriched liquid flow from the column system and for sending it vaporization means constituted by the main exchanger or independent vaporizer of the main exchanger, means for heating the oxygen-rich gas produced by the vaporization of the oxygen enriched liquid, these heating means being constituted by the main exchanger, means for sending all the air to be treated in the system of columns at a first axial portion of the main compressor for producing air at the pressure P1 of the medium pressure column, means for sending a first portion of the air substantially at the pressure of the medium pressure column to the middle column pressure, means for sending a second portion of the air substantially to the pressure of the medium pressure column to a second radial or centrifugal portion of the main compressor to bring it at least to a high pressure P2, means for sending the air at the high pressure from the second part to the main exchanger and possibly subsequently to the vaporizer, the first part and the second part part of the compressor being on the same shaft, in the same frame, and driven by the same drive means, such as an electric motor or one or more turbine (s).
Selon d'autres objets facultatifs, l'installation comprend :According to other optional objects, the installation includes:
- des moyens de séchage et/ou décarbonatation entre la sortie de la première partie et l'entrée de la deuxième partie ; - la première partie et la deuxième partie du compresseur sont chacune munie d'aubages directeurs ;means for drying and / or decarbonation between the outlet of the first part and the inlet of the second part; the first part and the second part of the compressor are each provided with guide vanes;
- une vanne de laminage installée en amont de l'entrée la deuxième partie ;a rolling valve installed upstream of the inlet the second part;
- la deuxième partie du compresseur comprend une première section et une deuxième section, des moyens pour envoyer toute la deuxième partie de l'air substantiellement à la moyenne pression à la première section pour la pressuriser à la pression élevée, des moyens pour diviser la deuxième partie de l'air en deux pour former un premier débit et un deuxième débit, des moyens pour envoyer le premier débit à l'échangeur principal et éventuellement au vaporiseur, des moyens pour envoyer le deuxième débit à la deuxième section pour la pressuriser à une pression haute plus élevée que la pression élevée et des moyens pour envoyer le deuxième débit à la pression haute à l'échangeur principal et ensuite à un vaporiseur de la colonne basse pression, de préférence à un vaporiseur de cuve de la colonne basse pression. Selon un autre objet de l'invention, il est prévu un procédé de séparation d'air produisant de l'oxygène gazeux à une pression inférieure à 5 bars abs, utilisant un système de colonnes comprenant au moins une colonne moyenne pression et au moins une colonne basse pression, un échangeur principal, un compresseur principal ayant des étages dans lequel : a) la totalité Q1 de l'air traité est comprimée jusqu'à une première pression P1 qui correspond à la pression de la colonne moyenne pression, aux pertes de charge près b) une partie Q2 de cet air à la pression P1 est surpressée jusqu'à une pression élevée P2, supérieure à P1 , qui permet la vaporisation d'oxygène liquide dans l'échangeur principal ou dans un vaporiseur dédié par échange de chaleur avec un débit d'oxygène liquide c) le débit d'oxygène liquide est soutiré de la colonne basse pression, éventuellement pressurisé à une pression inférieure à 5 bars abs, et envoyé à l'échangeur principal ou à un vaporiseur dédié où il se vaporise par échange de chaleur avec au moins la partie de l'air à la pression élevée P2 d) la totalité Q1 de l'air est comprimée dans une première partie axiale du compresseur constituée par au moins le premier étage du compresseur principal e) la partie Q2 de l'air à la pression P1 est surpressée dans une deuxième partie radiale ou centrifuge du compresseur jusqu'à la pression élevée P2 f) la valeur de Q2 est inférieur à Q1 d'au moins 33%, préférentiellement d'au moins 50% voire d'au moins 66%) g) la première partie et la deuxième partie du compresseur sont sur un même arbre, dans un même bâti et h) de l'énergie est fournie à la première et à la deuxième parties par le même moyen, constitué par au moins un moteur électrique et/ou au moins une turbine. Optionnellement :the second part of the compressor comprises a first section and a second section, means for sending all the second part of the air substantially at medium pressure to the first section to pressurize it at the high pressure, means for dividing the second section; part of the air in two to form a first flow and a second flow, means for sending the first flow to the main exchanger and possibly to the vaporizer, means for sending the second flow to the second section to pressurize it to a high pressure higher than the high pressure and means for sending the second flow at the high pressure to the main exchanger and then to a vaporizer of the low pressure column, preferably a tank vaporizer of the low pressure column. According to another object of the invention, there is provided an air separation method producing oxygen gas at a pressure of less than 5 bar abs, using a column system comprising at least one medium-pressure column and at least one low pressure column, a main exchanger, a main compressor having stages in which: a) the totality Q1 of the treated air is compressed to a first pressure P1 which corresponds to the pressure of the medium pressure column, to the losses of charge near b) a portion Q2 of this air at the pressure P1 is supercharged to a high pressure P2, greater than P1, which allows the vaporization of liquid oxygen in the main exchanger or in a dedicated vaporizer by heat exchange with a flow of liquid oxygen c) the flow of liquid oxygen is withdrawn from the low pressure column, possibly pressurized at a pressure of less than 5 bar abs, and sent to the main exchanger 1 or to a dedicated vaporizer where it vaporizes by heat exchange with at least the part of the air at the high pressure P2 d) the totality Q1 of the air is compressed in a first axial part of the compressor constituted by at least the first stage of the main compressor e) the part Q2 of the air at the pressure P1 is supercharged in a second radial or centrifugal part of the compressor up to the high pressure P2 f) the value of Q2 is less than Q1 of the minus 33%, preferably at least 50% or even at least 66%) g) the first part and the second part of the compressor are on the same shaft, in the same frame and h) energy is supplied to the first and second parts by the same means, consisting of at least one electric motor and / or at least one turbine. Optionally:
- la pression P1 est inférieure à 4.5 bar abs, préférablement inférieure à 4 bar, même encore inférieure à 3.5 bar abs ;the pressure P1 is less than 4.5 bar abs, preferably less than 4 bar, even less than 3.5 bar abs;
- la pression P2 est inférieure à 15 bar abs, préférablement inférieure à 10 bar, et encore inférieure à 6 bar abs ; - le débit de Q2 comprimé jusqu'à la pression P2 est inférieur à la moitié du débit de Q1 , et préférentiel lement inférieur à un tiers du débit de Q1 ;the pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs; the flow rate of Q2 compressed to the pressure P2 is less than half the flow rate of Q1, and preferably less than one third of the flow rate of Q1;
- la deuxième partie du compresseur principal comprend une première section et une deuxième section et dans lequel toute la partie Q2 de l'air est comprimé jusqu'à la pression P2 dans la première section, la partie Q2 est divisée en deux pour former un premier et un deuxième débit, le premier débit étant refroidi dans l'échangeur principal et éventuellement envoyé au vaporiseur à la pression élevée P2 et le deuxième débit étant surpressé jusqu'à une haute pression P3, plus élevée que la pression P2, refroidi à la haute pression dans l'échangeur principal et employé pour chauffer un vaporiseur de la colonne basse pression, de préférence le vaporiseur de cuve ;the second part of the main compressor comprises a first section and a second section and in which the whole part Q2 of the air is compressed to the pressure P2 in the first section, the part Q2 is divided in two to form a first section; and a second flow rate, the first flow rate being cooled in the main exchanger and optionally sent to the vaporizer at the high pressure P2 and the second flow rate being supercharged to a high pressure P3, higher than the pressure P2, cooled to the high pressure in the main exchanger and used to heat a vaporizer of the low pressure column, preferably the vessel vaporizer;
- une partie de l'air à la première pression P1 est envoyée à un vaporiseur intermédiaire de la colonne basse pression où elle se condense, l'air condensé étant envoyé à la colonne moyenne pression ; - on sèche la totalité Q1 de l'air traité comprimé jusqu'à une première pression P1 dans la première partie du compresseur.a part of the air at the first pressure P1 is sent to an intermediate vaporizer of the low pressure column where it condenses, the condensed air being sent to the medium pressure column; the whole Q1 of the compressed compressed air is dried up to a first pressure P1 in the first part of the compressor.
L'invention sera décrite en plus de détail en se référant aux figures qui illustrent un appareil de séparation d'air selon l'invention.The invention will be described in more detail with reference to the figures which illustrate an air separation apparatus according to the invention.
Dans la Figure 1 , l'appareil comprend une ligne d'échange 21 et une double colonne constituée par une colonne moyenne pression 27 et une colonne basse pression 29.In FIG. 1, the apparatus comprises an exchange line 21 and a double column constituted by a medium pressure column 27 and a low pressure column 29.
Tout l'air 1 est comprimé dans la première partie 3 d'un compresseur principal 4 constituée par au moins un étage axial pour produire de l'air à la pression P1 substantiellement égale à la pression de la colonne moyenne pression 27. La première partie comprend de préférence plusieurs étages, tous axiaux. L'air à la pression P1 est refroidi dans un refroidisseur 7 (qui peut être soit un échangeur tubulaire, soit une tour air/eau à un ou deux étages), épuré dans une unité d'épuration 9 et divisé en trois fractions. La première fraction 11 est surpressée dans au moins le dernier étage du compresseur principal, dernier étage qui fait partie de la deuxième partie du compresseur. Ce dernier étage et de préférence tous les étages de la deuxième partie sont des étages radiaux ou des étages centrifuges. Le compresseur principal avec sa première partie et sa deuxième constitue une machine unique à bâti unique et la première partie et la deuxième partie du compresseur sont entraînées par le même moyen, dans l'exemple un moteur M. La pression P1 est inférieure à 5 bars abs, voire à 4.5 bar abs, préférablement inférieure à 4 bar, et encore inférieure à 3.5 bar absAll the air 1 is compressed in the first part 3 of a main compressor 4 constituted by at least one axial stage to produce air at the pressure P1 substantially equal to the pressure of the medium pressure column 27. The first part preferably comprises several stages, all axial. The air at pressure P1 is cooled in a cooler 7 (which can be either a tubular exchanger or a tower air / water one or two stages), purified in a purification unit 9 and divided into three fractions. The first fraction 11 is supercharged in at least the last stage of the main compressor, the last stage which is part of the second part of the compressor. This last stage and preferably all the stages of the second part are radial stages or centrifugal stages. The main compressor with its first part and its second is a single machine with a single frame and the first part and the second part of the compressor are driven by the same way, in the example an engine M. The pressure P1 is less than 5 bar abs, or even 4.5 bar abs, preferably less than 4 bar, and still less than 3.5 bar abs
La première fraction 11 est amenée par la deuxième partie 5 du compresseur principal à une pression P2 et se refroidit à cette pression dans la ligne d'échange 21. La fraction 11 est ensuite envoyée à un vaporiseur 41 où elle se condense au moins partiellement avant d'être détendue et envoyée à la colonne moyenne pression 27. La pression P2 est inférieure à 15 bar abs, préférablement inférieure à 10 bar, et encore inférieure à 6 bar abs. La fraction 11 est inférieure à la moitié du débit 1 , et préférentiellement inférieure à un tiers du débit 1The first fraction 11 is fed by the second part 5 of the main compressor to a pressure P2 and cools to this pressure in the exchange line 21. The fraction 11 is then sent to a vaporizer 41 where it condenses at least partially before to be relaxed and sent to the medium pressure column 27. The pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs. Fraction 11 is less than half of flow 1, and preferentially less than one third of flow 1
La deuxième fraction 13 à la pression P1 se refroidit complètement dans la ligne d'échange 21 et est divisée en deux flux. Le premier flux 23 est envoyé à un rebouilleur de cuve 33 de la colonne basse pression 29 où il se condense au moins partiellement et est envoyé à la colonne moyenne pression, mélangé au débit 11. Le deuxième flux 25 est envoyé sous forme gazeuse à la colonne moyenne pression 27.The second fraction 13 at the pressure P1 cools completely in the exchange line 21 and is divided into two streams. The first stream 23 is sent to a bottom reboiler 33 of the low pressure column 29 where it condenses at least partially and is sent to the medium pressure column, mixed with the flow rate 11. The second stream 25 is sent in gaseous form to the medium pressure column 27.
La troisième fraction 15 est surpressée dans un surpresseur 17 entraîné par une turbine cryogénique 19, refroidie partiellement dans la ligne d'échange 21 , soutirée de la ligne d'échange à un niveau intermédiaire de celle-ci et détendue dans la turbine 19 avant d'être envoyée à la colonne basse pressionThe third fraction 15 is supercharged in a booster 17 driven by a cryogenic turbine 19, partially cooled in the exchange line 21, withdrawn from the exchange line at an intermediate level thereof and expanded in the turbine 19 before to be sent to the low pressure column
29.29.
Un débit de liquide enrichi en oxygène 55, un débit intermédiaire 53 et un débit liquide riche en azote 51 sont soutirés de la colonne moyenne pression 27, refroidis dans l'échangeur 31 , détendus et envoyés à des niveaux différents de la colonne basse pression 29.An oxygen-enriched liquid flow 55, an intermediate flow 53 and a nitrogen-rich liquid flow 51 are withdrawn from the medium-pressure column 27, cooled in the exchanger 31, expanded and sent to different levels of the low-pressure column 29 .
De l'azote gazeux moyenne pression 49 est condensé dans un vaporiseur intermédiaire 35 de la colonne basse pression 29 et envoyé comme reflux en tête de la colonne moyenne pression 27. Un autre débit d'azote gazeux moyenne pression 47 se réchauffe dans la ligne d'échange.Medium pressure nitrogen gas 49 is condensed in an intermediate vaporizer 35 of the low pressure column 29 and sent as reflux to the top of the medium pressure column 27. Another flow of medium pressure nitrogen gas 47 is heated in the line of 'exchange.
De l'oxygène liquide 37 est soutiré en cuve de la colonne basse pression 29, pressurisé par une pompe 39 à une pression inférieure à 5 bars abs et envoyé au vaporiseur 41. A part une purge de liquide 43, l'oxygène se vaporise dans le vaporiseur 41 par échange de chaleur avec la fraction d'air 11 à la pression P2. L'oxygène forme ensuite le débit d'oxygène gazeux pressurisé 45 qui se réchauffe dans la ligne d'échange 21.Liquid oxygen 37 is withdrawn in the bottom of the low pressure column 29, pressurized by a pump 39 at a pressure lower than 5 bar abs and sent to the vaporizer 41. Apart from a liquid purge 43, the oxygen vaporizes in the vaporizer 41 by heat exchange with the air fraction 11 to the P2 pressure. The oxygen then forms the flow rate of pressurized gaseous oxygen 45 which heats up in the exchange line 21.
Dans la Figure 2, l'appareil comprend une ligne d'échange 21 et une double colonne constituée par une colonne moyenne pression 27 et une colonne basse pression 29. La colonne basse pression diffère de celle de la Figure 1 en ce qu'elle a trois vaporiseurs 33, 34,35 au lieu de deux.In FIG. 2, the apparatus comprises an exchange line 21 and a double column formed by a medium pressure column 27 and a low pressure column 29. The low pressure column differs from that of FIG. three vaporizers 33, 34.35 instead of two.
Tout l'air 1 est comprimé dans la première partie 3 d'un compresseur principal 4 constituée par au moins un étage axial pour produire de l'air à la pression P1 substantiellement égale à la pression de la colonne moyenne pression 27. La première partie comprend de préférence plusieurs étages, tous axiaux. L'air à la pression P1 est refroidi dans un refroidisseur 7, épuré dans une unité d'épuration 9 et divisé en trois fractions. La première fraction 11 est surpressée dans la première section 5A de la deuxième partie du compresseur principal 4. La première section 5A est composée de préférence entièrement d'étages radiaux ou centrifuges. Le compresseur principal avec sa première partie et sa deuxième partie, en deux sections, constitue une machine unique à bâti unique et la première partie et la deuxième partie du compresseur sont entraînées par le même moyen, dans l'exemple un moteur M. La pression P1 est inférieure à 5 bars abs, voire à 4.5 bar abs, préférablement inférieure à 4 bar, et encore inférieure à 3.5 bar absAll the air 1 is compressed in the first part 3 of a main compressor 4 constituted by at least one axial stage to produce air at the pressure P1 substantially equal to the pressure of the medium pressure column 27. The first part preferably comprises several stages, all axial. The air at pressure P1 is cooled in a cooler 7, purified in a purification unit 9 and divided into three fractions. The first fraction 11 is supercharged in the first section 5A of the second part of the main compressor 4. The first section 5A is preferably composed entirely of radial or centrifugal stages. The main compressor with its first part and its second part, in two sections, is a single machine with a single frame and the first part and the second part of the compressor are driven by the same means, in the example an engine M. The pressure P1 is less than 5 bar abs, even 4.5 bar abs, preferably less than 4 bar, and still less than 3.5 bar abs
La première fraction 11 est amenée par la première section 5A de la deuxième partie du compresseur principal à une pression élevée P2 et se divise en deux débits. Le premier débit 26 se refroidit à cette pression P2 dans la ligne d'échange 21. Le premier débit 26 est ensuite envoyé à un vaporiseur 41 où il se condense au moins partiellement avant d'être détendu et envoyé à la colonne moyenne pression 27. La pression P2 est inférieure à 15 bar abs, préférablement inférieure à 10 bar, et encore inférieure à 6 bar abs. La première fraction 11 est inférieure à la moitié du débit 1 , et préférentiellement inférieure à un tiers du débit 1. Le deuxième débit 23 est surpressé à une haute pression P3 dans la deuxième section 5B de la deuxième partie d u compresseur 4. La deuxième section 5B est composée, de préférence entièrement, du même type d'étages que la première section 5A, que ce soit des étages radiaux ou centrifuges. Le débit 23 à la haute pression se refroidit dans l'échangeur principal 21 et est envoyé au vaporiseur 33 en cuve de la colonne basse pression 29. Il est également envisageable d'envoyer ce débit à un des vaporiseur supérieurs 34,35. Là le débit 23 se condense au moins partiellement et est envoyé être mélangé avec le débit 26 condensé dans le vaporiseur 41. La deuxième fraction 13 à la pression P1 se refroidit complètement dans la ligne d'échange 21 et est divisée en deux flux. Le premier flux 24 est envoyé à un vaporiseur intermédiaire 34 de la colonne basse pression 29 où il se condense au moins partiellement et est envoyé à la colonne moyenne pression, mélangé au débit 26. Le deuxième flux 25 est envoyé sous forme gazeuse à la colonne moyenne pression 27.The first fraction 11 is fed through the first section 5A of the second part of the main compressor at a high pressure P2 and divides into two flow rates. The first flow 26 cools at this pressure P2 in the exchange line 21. The first flow 26 is then sent to a vaporizer 41 where it condenses at least partially before being expanded and sent to the medium pressure column 27. The pressure P2 is less than 15 bar abs, preferably less than 10 bar, and still less than 6 bar abs. The first fraction 11 is less than half the flow 1, and preferably less than one-third of the flow 1. The second flow 23 is supercharged at a high pressure P3 in the second section 5B of the second part of the compressor 4. The second section 5B is composed, preferably entirely, of the same type of stages as the first section 5A, whether it is radial or centrifugal stages. The flow 23 at the high pressure cools in the main exchanger 21 and is sent to the vaporizer 33 in the tank of the low pressure column 29. It is also possible to send this flow to one of the upper vaporizer 34,35. There the flow 23 condenses at least partially and is sent to be mixed with the flow 26 condensed in the vaporizer 41. The second fraction 13 at the pressure P1 cools completely in the exchange line 21 and is divided into two streams. The first stream 24 is sent to an intermediate vaporizer 34 of the low pressure column 29 where it condenses at least partially and is sent to the medium pressure column, mixed with the flow rate 26. The second stream 25 is sent in gaseous form to the column medium pressure 27.
La troisième fraction 15 est surpressée dans un surpresseur 17 entraîné par une turbine cryogénique 19, refroidie partiellement dans la ligne d'échange 21 , soutirée de la ligne d'échange à un niveau intermédiaire de celle-ci et détendue dans la turbine 19 avant d'être envoyée à la colonne basse pression 29.The third fraction 15 is supercharged in a booster 17 driven by a cryogenic turbine 19, partially cooled in the exchange line 21, withdrawn from the exchange line at an intermediate level thereof and expanded in the turbine 19 before to be sent to the low pressure column 29.
Un débit de liquide enrichi en oxygène 55, un débit intermédiaire 53 et un débit liquide riche en azote 51 sont soutirés de la colonne moyenne pression 27, refroidis dans l'échangeur 31 , détendus et envoyés à des niveaux différents de la colonne basse pression 29. De l'azote gazeux moyenne pression 49 est condensé dans u n vaporiseur supérieur 35 de la colonne basse pression 29 et envoyé comme reflux en tête de la colonne moyenne pression 27.An oxygen-enriched liquid flow 55, an intermediate flow 53 and a nitrogen-rich liquid flow 51 are withdrawn from the medium-pressure column 27, cooled in the exchanger 31, expanded and sent to different levels of the low-pressure column 29 Medium pressure nitrogen gas 49 is condensed in an upper vaporizer 35 of the low pressure column 29 and sent as reflux to the top of the medium pressure column 27.
De l'oxygène liquide 37 est soutiré en cuve de la colonne basse pression 29, pressurisé par une pompe 39 à une pression inférieure à 5 bars abs et envoyé au vaporiseur 41. A part une purge de liquide 43, l'oxygène se vaporise dans le vaporiseur 41 par échange de chaleur avec le débit d'air 26 à la pression P2. L'oxygène forme ensuite le débit d'oxygène gazeux pressurisé 45 qui se réchauffe dans la ligne d'échange 21 , qui est le produit principal de l'appareil. Alors que les figures précédentes illustrent des doubles colonnes, il est envisageable de scinder la colonne basse pression en deux, voire trois (cas de Figure 2) pour réduire la hauteur de colonnes. De même la colonne moyenne pression peut être placée à côté de la ou les colonne(s) basse pression. Il est également concevable d'utiliser l'invention dans le contexte d'une triple colonne, en rajoutant une colonne opérant à une pression intermédiaire entre celles de la colonne moyenne pression et de la colonne basse pression, cette colonne étant alimenté par du liquide riche vaporisé et/ou de l'air, et peut opérer éventuellement en parallèle de la colonne moyenne pression décrite précédemmentLiquid oxygen 37 is withdrawn in the bottom of the low pressure column 29, pressurized by a pump 39 at a pressure lower than 5 bar abs and sent to the vaporizer 41. Apart from a liquid purge 43, the oxygen vaporizes in the vaporizer 41 by heat exchange with the air flow 26 at the pressure P2. The oxygen then forms the rate of pressurized oxygen gas 45 which heats up in the exchange line 21, which is the main product of the apparatus. While the preceding figures illustrate double columns, it is conceivable to split the low pressure column into two or even three (as in Figure 2) to reduce the height of columns. Similarly the medium pressure column can be placed next to the low pressure column (s). It is also conceivable to use the invention in the context of a triple column, by adding a column operating at a pressure intermediate between those of the medium pressure column and the low pressure column, this column being fed with vaporized rich liquid and / or air, and may optionally operate in parallel with the medium pressure column previously described
II est aussi possible de remplacer ou complémenter la détente d'air en turbine d'insufflation par une détente d'azote moyenne pression et/ou une détente d'air jusqu'à la pression de la colonne moyenne pression dans une turbine communément appelée turbine Claude. Dans le cas des deux figures, le compresseur peut être contrôlé par des aubages directeurs dont sont munies la première et la deuxième partie. Sinon une vanne de laminage peut être placée à l'entrée de la deuxième partie du compresseur, pour contrôler la deuxième partie du compresseur. It is also possible to replace or supplement the air expansion blowing turbine by a relaxation of medium pressure nitrogen and / or an expansion of air to the pressure of the medium pressure column in a turbine commonly called turbine Claude. In the case of both figures, the compressor can be controlled by guide vanes which are provided with the first and second part. Otherwise a rolling valve can be placed at the inlet of the second part of the compressor, to control the second part of the compressor.
Claims
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| FR0901488A FR2943772A1 (en) | 2009-03-27 | 2009-03-27 | APPARATUS AND METHOD FOR AIR SEPARATION BY CRYOGENIC DISTILLATION |
| FR0901488 | 2009-03-27 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| WO2010109149A2 true WO2010109149A2 (en) | 2010-09-30 |
| WO2010109149A3 WO2010109149A3 (en) | 2011-09-15 |
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| Application Number | Title | Priority Date | Filing Date |
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| PCT/FR2010/050550 Ceased WO2010109149A2 (en) | 2009-03-27 | 2010-03-25 | Apparatus and method for separating air by cryogenic distillation |
Country Status (2)
| Country | Link |
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| FR (1) | FR2943772A1 (en) |
| WO (1) | WO2010109149A2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012127148A2 (en) | 2011-03-18 | 2012-09-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device and method for separating air by cryogenic distillation |
| CN103842753A (en) * | 2011-04-08 | 2014-06-04 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for separating air by cryogenic distillation |
| CN104251599A (en) * | 2014-07-12 | 2014-12-31 | 孙竟成 | Ultralow pressure air separation plant process flow |
| CN104067079B (en) * | 2011-03-18 | 2016-11-30 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and method for separating air by cryogenic distillation |
| CN109387031A (en) * | 2017-08-03 | 2019-02-26 | 乔治洛德方法研究和开发液化空气有限公司 | Device and method for separating air by low temperature distillation |
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| US2828066A (en) * | 1954-07-05 | 1958-03-25 | Sulzer Ag | Turbocompressor plant |
| GB9325648D0 (en) * | 1993-12-15 | 1994-02-16 | Boc Group Plc | Air separation |
| FR2721383B1 (en) * | 1994-06-20 | 1996-07-19 | Maurice Grenier | Process and installation for producing gaseous oxygen under pressure. |
| EP0793069A1 (en) * | 1996-03-01 | 1997-09-03 | Air Products And Chemicals, Inc. | Dual purity oxygen generator with reboiler compressor |
| GB9801200D0 (en) * | 1998-01-20 | 1998-03-18 | Air Prod & Chem | Intergration of a cryogenic air separator with synthesis gas production and conversion |
| FR2827186A1 (en) * | 2001-07-12 | 2003-01-17 | Air Liquide | Compressor(s) in an air distillation unit supplying gas(es) to an industrial unit which produces steam are driven using the steam from the industrial unit and an electric motor |
| FR2898645B1 (en) * | 2006-03-14 | 2008-08-22 | L'air Liquide | MULTI-STAGE COMPRESSOR, AIR SEPARATION APPARATUS COMPRISING SUCH A COMPRESSOR AND INSTALLATION |
| US8047809B2 (en) * | 2007-04-30 | 2011-11-01 | General Electric Company | Modular air compression apparatus with separate platform arrangement |
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- 2009-03-27 FR FR0901488A patent/FR2943772A1/en active Pending
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| RAMSDOHR: "Optimize air compressor performance for GTL Plants", HYDROCARBON PROCESSING, January 2004 (2004-01-01) |
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2012127148A2 (en) | 2011-03-18 | 2012-09-27 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device and method for separating air by cryogenic distillation |
| US20130340476A1 (en) * | 2011-03-18 | 2013-12-26 | L'air Liquide Societe Anonyme Pour I'etude Et I'exploitation Des Procedes Georges Claude | Apparatus and method for separating air by cryogenic distillation |
| CN104067079A (en) * | 2011-03-18 | 2014-09-24 | 乔治洛德方法研究和开发液化空气有限公司 | Device and method for separating air by cryogenic distillation |
| WO2012127148A3 (en) * | 2011-03-18 | 2014-12-04 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device and method for separating air by cryogenic distillation |
| CN104067079B (en) * | 2011-03-18 | 2016-11-30 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and method for separating air by cryogenic distillation |
| AU2012230171B2 (en) * | 2011-03-18 | 2017-03-30 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Device and method for separating air by cryogenic distillation |
| CN103842753A (en) * | 2011-04-08 | 2014-06-04 | 乔治洛德方法研究和开发液化空气有限公司 | Method and device for separating air by cryogenic distillation |
| WO2012136939A3 (en) * | 2011-04-08 | 2015-01-22 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Method and device for separating air by cryogenic distillation |
| CN103842753B (en) * | 2011-04-08 | 2016-12-07 | 乔治洛德方法研究和开发液化空气有限公司 | For by the method and apparatus of separating air by cryogenic distillation |
| CN104251599A (en) * | 2014-07-12 | 2014-12-31 | 孙竟成 | Ultralow pressure air separation plant process flow |
| CN109387031A (en) * | 2017-08-03 | 2019-02-26 | 乔治洛德方法研究和开发液化空气有限公司 | Device and method for separating air by low temperature distillation |
| CN109387031B (en) * | 2017-08-03 | 2021-11-02 | 乔治洛德方法研究和开发液化空气有限公司 | Apparatus and method for separating air by cryogenic distillation |
Also Published As
| Publication number | Publication date |
|---|---|
| FR2943772A1 (en) | 2010-10-01 |
| WO2010109149A3 (en) | 2011-09-15 |
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