EP3343159A1 - Procédé et dispositif de production d'oxygène gazeux et azote comprimé gazeux - Google Patents

Procédé et dispositif de production d'oxygène gazeux et azote comprimé gazeux Download PDF

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Publication number
EP3343159A1
EP3343159A1 EP16020518.3A EP16020518A EP3343159A1 EP 3343159 A1 EP3343159 A1 EP 3343159A1 EP 16020518 A EP16020518 A EP 16020518A EP 3343159 A1 EP3343159 A1 EP 3343159A1
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Prior art keywords
pressure column
nitrogen
low
pressure
oxygen
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EP16020518.3A
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German (de)
English (en)
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Dimitri GOLUBEV
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Linde GmbH
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Linde GmbH
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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
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—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
    • F25J3/04054—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 air
    • 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
    • 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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    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04103—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression using solely hydrostatic liquid head
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    • 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
    • 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
    • F25J3/04296—Claude expansion, i.e. expanded into the main or high pressure column
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • 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
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    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • F25J3/04309—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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    • 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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    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04393—Details relating to the work expansion, e.g. process parameter etc. using multiple or multistage gas work expansion
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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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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    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column
    • F25J2200/54—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the column in the low pressure column of a double pressure main column system
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    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/54—Oxygen production with multiple pressure O2
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
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    • F25J2235/42—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being nitrogen
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    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/12—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being nitrogen
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Definitions

  • the invention relates to a method according to the preamble of patent claim 1.
  • the invention relates in particular to gas and steam power plants (CCGT), internationally most commonly referred to as IGCC (Integrated Gasification Combined Cycle).
  • CCGT gas and steam power plants
  • IGCC Integrated Gasification Combined Cycle
  • the present invention relates to processes involving relatively high pressure GAN, namely from 0.7.2 to about 1.5 times the amount of oxygen product. So far, this requirement has been conventionally solved, for example, with a double-column method with removal of the pressure GAN from the high-pressure column and injection turbine, ie the introduction of turbine-relaxed air into the low-pressure column, for generating the process refrigeration; Here one achieves only a relatively poor oxygen yield and requires a lot of feed air.
  • Another method employing a dual column method of removing the pressure GAN from the high pressure column includes a low pressure GAN reboiler and an injection turbine for refrigeration. Here also an additional machine is used.
  • the invention is therefore based on the object to find a method which not only efficiently generates the desired product combination, but also requires relatively low investment costs.
  • Refrigeration production is further improved by heating the nitrogen-enriched intermediate fraction upstream of the work-performing expansion.
  • it is heated in the main heat exchanger to an intermediate temperature of, for example, 100 to 120 K, preferably 100 to 110 K.
  • the low-pressure column intermediate evaporator has a particularly efficient evaporation. This is made possible in particular by being designed either as a forced-flow evaporator or as a falling-film evaporator.
  • the entire feed air is compressed in all stages of a three-stage main air compressor to its final pressure.
  • the three-stage main air compressor is the only machine that operates on external energy.
  • the oxygen fraction can be withdrawn directly in gaseous form from the low-pressure column, warmed in the main heat exchanger and recovered as a product.
  • the oxygen fraction is removed in the liquid state from the lower region of the low pressure column and the heating in the main heat exchanger in a secondary condenser, which is designed as a condenser-evaporator, is vaporized in indirect heat exchange with a partial flow of the feed air .
  • the secondary condenser causes a slight increase in the discharge pressure, for example by 0.2 bar and a slight increase in the oxygen content, without the additional energy would be expended.
  • high-pressure oxygen can also be obtained by internal compression of the low-pressure column bottoms liquid or of the liquid from the evaporation space of a secondary condenser.
  • the invention also relates to a device according to claim 10.
  • the device according to the invention can be supplemented by device features that correspond to the characteristics of individual, several or all dependent method claims.
  • atmospheric air (AIR) 1 is compressed via a filter 2 by a three-stage main air compressor 3 with intermediate cooling (not shown).
  • the compressed to about 5.5 bar feed air 4 is further treated in a pre-cooling 5 and a cleaning device 6.
  • the compressed and purified feed air 7 is introduced into a main heat exchanger 8 and cooled there to about dew point.
  • a first portion 10 of the cooled feed air is introduced directly into the high pressure column 11 of a distillation column system for nitrogen-oxygen separation.
  • the distillation column system for nitrogen-oxygen separation also comprises a low-pressure column 12, a main condenser 13 and a low-pressure column intermediate evaporator 14.
  • the two capacitors 13, 14 are each formed as a condenser-evaporator.
  • a second part 15 of the cooled feed air 9 flows through the liquefaction space of a secondary condenser 16, which is likewise designed as a condenser-evaporator and functions as a bath evaporator.
  • the completely or partially liquefied air 17 is supplied to the high-pressure column 11 at an intermediate point. At least a portion 18 of the liquid air is removed again, cooled in a supercooling countercurrent 19 and fed via line 20 of the low pressure column 12.
  • Liquid crude oxygen 21 of the high pressure column 11 is also supercooled in the subcooler countercurrent 19 and then flows via line 22 to the low pressure column 12.
  • Gaseous overhead nitrogen 23 of the high pressure column 11 is completely or almost completely liquefied to a first part 24 in the main condenser.
  • a second part 35 of the gaseous top nitrogen 23 of the high pressure column 11 is warmed in the main heat exchanger 8 and recovered via line 36 as gaseous pressure nitrogen product (PGAN).
  • GPN gaseous pressure nitrogen product
  • a nitrogen-enriched intermediate fraction 26 of the high-pressure column 11 has a nitrogen content of 99 mol% in the example.
  • the warmed intermediate fraction 27 is expanded in an expansion turbine 28 to perform work and then introduced via line 29 into the liquefaction chamber of the low-pressure column intermediate evaporator 14.
  • the turbine 28 is braked by an electric generator.
  • a dissipative brake such as an oil brake could be used.
  • the partially or completely liquefied impure nitrogen 30 is returned according to the invention by means of a pump 31 via line 32 into the high-pressure column 11.
  • the introduction takes place in this illustration in the supercooled state; Alternatively, the stream 32 may be heated prior to its introduction into the high pressure column 11 in the subcooling countercurrent 19 or in a separate subcooling countercurrent.
  • a portion of the fed into the high-pressure column 11 liquid is removed via line 33 again from the high pressure column 11, cooled in the subcooling countercurrent 19 and fed via line 34 of the low pressure column 12 as a head return.
  • the evaporation space of the low-pressure column intermediate evaporator 14 is designed as a forced-flow evaporator. In these, the entire reflux liquid of the low-pressure column 12 is introduced. The liquid remaining portion (L) continues to flow down the low pressure column 12, the vaporized portion (V) flows back into the upper part of the low pressure column 12th
  • an oxygen fraction 37 having an oxygen content of Withdrawn liquid 92.2 mol% passed into the arranged a few meters lower side condenser 16 and there for the most part evaporated under a pressure and with an oxygen content of 95 mol% for the most part.
  • the vaporized oxygen 38 is warmed in the main heat exchanger 8 to about ambient temperature and is recovered via line 39 as a gaseous oxygen product Unoxygen (GOX).
  • GOX gaseous oxygen product Unoxygen
  • a small amount of purging is taken continuously or from time to time via the purge line 40 liquid from the evaporation space of the secondary condenser 16 and introduced into the warm oxygen stream 39. Alternatively, this stream can be brought to supercritical pressure in a pump, heated in the heat exchanger and fed to the oxygen stream 39.
  • impure nitrogen 41 is removed as residual gas and used after heating in supercooling countercurrent 19 and main heat exchanger 8 via line 42 either as a regeneration for the cleaning device 6, used as dry gas in an evaporative cooler or discarded.
  • FIG. 1a only differs from this FIG. 1 in that only a portion 30a of the liquid nitrogen 30 from the low pressure column intermediate evaporator 14 in pump 31 is brought to something above high pressure column pressure.
  • the remainder 30b forms the return liquid for the low pressure column 12 and is cooled as usual in the subcooling countercurrent 19 and fed via line 34 to the top of the low pressure column 12.
  • a first portion 243 is brought to an increased product pressure in an oxygen pump 244, which may be supercritical or subcritical.
  • the high pressure oxygen 245 is fed to the main heat exchanger 8 where it is vaporized (or pseudo vaporized at supercritical pressure) and warmed to ambient temperature.
  • the high pressure oxygen product (GOXIV1) is recovered.
  • a second part 241 of the liquid 240 is obtained - optionally after subcooling in the subcooling countercurrent 19 via line 242 as liquid nitrogen product (LOX).
  • a liquid nitrogen product (LIN) is further recovered from a portion of the nitrogen 225 condensed in the main condenser 13.
  • FIG. 3 Compared to FIG. 2 allows the embodiment of FIG. 3 higher product pressures or larger quantities in the internally compressed product 243, 244, 245, 246 (GOXIV1);
  • an external energy driven air compressor (BAC) 303 is used, which brings a portion 307 of the compressed and cleaned air to a pressure which is significantly higher than the operating pressure of the high pressure column 11.
  • the cold compressor 403 is driven by a second expansion machine, namely an air turbine 450, which injects a portion 451 of the feed air into the low-pressure column 12 (line 452).
  • FIG. 4 Something similar will be in FIG. 4 achieved, but without the consumption of external energy.
  • a part 407 of the Einsetz Kunststoff is recompressed in a cold compressor 403.
  • the post-compressed air is introduced after cooling via line 315 in the liquefaction space of the secondary condenser 16. This is operated altogether at elevated pressure by increasing the pressure of the oxygen 37 for the evaporation side in a pump 444.
  • FIG. 5 the total air in the main air compressor 3 is compressed to a pressure which is at least 3 bar above the operating pressure of the high-pressure column 11.
  • the embodiment is similar FIG. 3
  • the re-compaction is like in FIG. 1 made by turbine-driven machines, namely by two serially connected cold compressors 555, 556.
  • the second cold compressor 556 is in turn driven by a Einblaseturbine 551, ie by an air turbine, which relaxes in the low-pressure column 12.
  • the first cold compressor 555 is coupled to a medium-pressure turbine 552, ie with an air turbine, which relaxes in the high-pressure column 11.
  • the expansion machine 28 is operated not with an intermediate fraction, but with gaseous nitrogen from the top of the high-pressure column 11; However, the remaining features of claim 1 are met here as well.
EP16020518.3A 2016-12-28 2016-12-28 Procédé et dispositif de production d'oxygène gazeux et azote comprimé gazeux Withdrawn EP3343159A1 (fr)

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EP16020518.3A EP3343159A1 (fr) 2016-12-28 2016-12-28 Procédé et dispositif de production d'oxygène gazeux et azote comprimé gazeux

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EP16020518.3A EP3343159A1 (fr) 2016-12-28 2016-12-28 Procédé et dispositif de production d'oxygène gazeux et azote comprimé gazeux

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112805524A (zh) * 2018-10-23 2021-05-14 林德有限责任公司 用于低温分离空气的方法和设备
CN115790077A (zh) * 2023-02-03 2023-03-14 杭氧集团股份有限公司 一种制造高纯氮和超纯氧的装置及其使用方法

Citations (4)

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Publication number Priority date Publication date Assignee Title
WO1988000677A1 (fr) * 1986-07-15 1988-01-28 Donald Erickson Refroidissement d'azote par detente partielle pour la separation cryogenique d'air
US5678427A (en) 1996-06-27 1997-10-21 Praxair Technology, Inc. Cryogenic rectification system for producing low purity oxygen and high purity nitrogen
US5956974A (en) * 1998-01-22 1999-09-28 Air Products And Chemicals, Inc. Multiple expander process to produce oxygen
US5966967A (en) * 1998-01-22 1999-10-19 Air Products And Chemicals, Inc. Efficient process to produce oxygen

Patent Citations (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1988000677A1 (fr) * 1986-07-15 1988-01-28 Donald Erickson Refroidissement d'azote par detente partielle pour la separation cryogenique d'air
US5678427A (en) 1996-06-27 1997-10-21 Praxair Technology, Inc. Cryogenic rectification system for producing low purity oxygen and high purity nitrogen
US5956974A (en) * 1998-01-22 1999-09-28 Air Products And Chemicals, Inc. Multiple expander process to produce oxygen
US5966967A (en) * 1998-01-22 1999-10-19 Air Products And Chemicals, Inc. Efficient process to produce oxygen

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN112805524A (zh) * 2018-10-23 2021-05-14 林德有限责任公司 用于低温分离空气的方法和设备
CN112805524B (zh) * 2018-10-23 2022-12-06 林德有限责任公司 用于低温分离空气的方法和设备
CN115790077A (zh) * 2023-02-03 2023-03-14 杭氧集团股份有限公司 一种制造高纯氮和超纯氧的装置及其使用方法

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