Nothing Special   »   [go: up one dir, main page]

EP2551619A1 - Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air - Google Patents

Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air Download PDF

Info

Publication number
EP2551619A1
EP2551619A1 EP11006132A EP11006132A EP2551619A1 EP 2551619 A1 EP2551619 A1 EP 2551619A1 EP 11006132 A EP11006132 A EP 11006132A EP 11006132 A EP11006132 A EP 11006132A EP 2551619 A1 EP2551619 A1 EP 2551619A1
Authority
EP
European Patent Office
Prior art keywords
pressure
column
nitrogen
low
oxygen
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP11006132A
Other languages
German (de)
English (en)
Inventor
Alexander Dr. Alekseev
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Original Assignee
Linde GmbH
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP11006132A priority Critical patent/EP2551619A1/fr
Priority to CN201210319498.9A priority patent/CN102901322B/zh
Priority to US13/558,529 priority patent/US20130047666A1/en
Publication of EP2551619A1 publication Critical patent/EP2551619A1/fr
Withdrawn legal-status Critical Current

Links

Images

Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • 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
    • F25J3/04084—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 nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—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
    • 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
    • F25J3/04375—Details relating to the work expansion, e.g. process parameter etc.
    • F25J3/04387—Details relating to the work expansion, e.g. process parameter etc. using liquid or hydraulic turbine expansion
    • 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
    • F25J3/04436—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 at least a triple pressure main column system
    • F25J3/04454—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 at least a triple pressure main column system a main column system not otherwise provided, e.g. serially coupling of columns or more than three pressure levels
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/10—Processes or apparatus using separation by rectification in a quadruple, or more, column or pressure system
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/20—Processes or apparatus using separation by rectification in an elevated pressure multiple column system wherein the lowest pressure column is at a pressure well above the minimum pressure needed to overcome pressure drop to reject the products to atmosphere
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2200/00—Processes or apparatus using separation by rectification
    • F25J2200/50—Processes or apparatus using separation by rectification using multiple (re-)boiler-condensers at different heights of the 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
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/52—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen enriched compared to air ("crude oxygen")
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/02—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream
    • F25J2240/10—Expansion of a process fluid in a work-extracting turbine (i.e. isentropic expansion), e.g. of the feed stream the fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/44—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being nitrogen
    • 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
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/40—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval
    • F25J2240/46—Expansion without extracting work, i.e. isenthalpic throttling, e.g. JT valve, regulating valve or venturi, or isentropic nozzle, e.g. Laval the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/20—Boiler-condenser with multiple exchanger cores in parallel or with multiple re-boiling or condensing streams

Definitions

  • the invention relates to a process for obtaining compressed nitrogen and pressure oxygen by cryogenic separation of air according to the preamble of patent claim 1.
  • the distillation column system of the invention may be designed as a two-column system (for example as a classic Linde double column system), or as a triple or multi-column system. It may in addition to the columns for nitrogen-oxygen separation, further devices for obtaining high purity products and / or other air components, in particular of noble gases, for example, an argon production and / or a krypton-xenon recovery.
  • printed product pressure oxygen product, compressed nitrogen product
  • pressure oxygen product compressed nitrogen product
  • Unreactive nitrogen refers to a fraction containing at least 80% nitrogen. These and all other percentages are to be understood as molar amounts.
  • the "main heat exchanger” is used to cool feed air in indirect heat exchange with backflow from the distillation column system for nitrogen-oxygen separation (or from other columns).
  • the main heat exchanger may be formed of one or more parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • condenser-evaporator refers to a heat exchanger in which a first condensing fluid stream undergoes indirect heat exchange with a second evaporating fluid stream.
  • Each condenser-evaporator has a liquefaction space and an evaporation space, which consist of liquefaction passages or evaporation passages.
  • the condensation (liquefaction) of a first fluid flow is performed, in the evaporation space the evaporation of a second fluid flow.
  • Evaporation and liquefaction space are formed by groups of passages that are in heat exchange relationship with each other.
  • the inventive method is particularly suitable for systems for the simultaneous production of pressure oxygen and large amounts of pressurized nitrogen; For example, 50 to 70% of the total amount of air is recovered as pressurized nitrogen. It can also be more pressure nitrogen fractions are produced at different pressures when they are needed by nitrogen consumers, as occurs for example in IGCC plants (gas and steam turbine power plant with integrated coal or heavy oil gasification).
  • IGCC plants gas and steam turbine power plant with integrated coal or heavy oil gasification
  • residual gas impurity nitrogen stream 10 to 30% of the total amount of air
  • residual gas impurity nitrogen stream 10 to 30% of the total amount of air
  • energy of this gas should be utilized in the plant.
  • the conventional solution is that the residual gas in a Heat exchanger is heated, then in a turbine (residual gas turbine) is relaxed to a corresponding low pressure. The residual gas cools down. The cold residual gas is passed through the main heat exchanger and cools warmer streams.
  • Such processes are over EP 384483 B1 ( US 5036672 ) or US 3886758 known.
  • the invention is therefore based on the object to provide a method of the type mentioned above and a corresponding device, which are economically particularly favorable and require relatively low investment costs and / or provide a particularly high stability during operation, especially at relatively low energy consumption.
  • residual gas column To recover the pressure energy from the impure nitrogen stream, an additional separation column is used instead of the residual gas turbine, which is referred to as residual gas column.
  • the impure nitrogen stream from the low-pressure column is first liquefied in an additional condenser-evaporator, which is located in the bottom of the residual gas column and then expanded in a throttle valve to the required low pressure.
  • the expanded liquid is passed from above into this additional separation column and serves as reflux for the separation process.
  • this additional separation column is cooled from above, it is heated from below by the sump heater.
  • This column is used to pre-separate the crude oxygen liquid from the bottom of the high pressure column. (In a three-column system may additionally or alternatively at least a portion of the bottom liquid of the medium-pressure column be introduced.)
  • This liquid is fed approximately in the middle of the column ("first intermediate point" of the residual gas column).
  • the gas from the residual gas column is then at a correspondingly low pressure.
  • the bottom liquid is oxygen-rich than the crude oxygen from the high-pressure column and can be fed at a corresponding point in another column of the distillation column system for nitrogen-oxygen separation.
  • the distillation column system for nitrogen-oxygen separation preferably has a main condenser, which is designed as a condenser-evaporator. About him are the head of the high pressure column and the bottom of the low pressure column in heat exchanging connection.
  • a liquid sump fraction is taken from the residual gas column and the low pressure column is fed to a second intermediate point, which is below the first intermediate point. Since the residual gas column is operated at a lower pressure than the low-pressure column, the pressure in the liquid bottom fraction must be increased before it is introduced into the low-pressure column, for example by a pump.
  • a gaseous residual stream is withdrawn from the top of the residual gas column and warmed in the main heat exchanger.
  • no increase in pressure is carried out in the impure nitrogen stream between the low-pressure column and the bottom evaporator, and in particular the liquefaction space of the bottom evaporator is operated substantially below the operating pressure of the low-pressure column.
  • the pressure oxygen product may in principle be recovered under the operating pressure of the low pressure column (minus line losses) or further compressed downstream of the main heat exchanger in an oxygen compressor
  • At least a portion of the (pseudo) liquefied feed air can be supplied to the residual gas column in this case, namely at a second intermediate point, which is above the first intermediate point at which the crude oxygen fraction is introduced from the high-pressure column.
  • the low-pressure column preferably has no top condenser.
  • the reflux liquid in the upper region of the residual gas column is in particular formed exclusively by the expanded impure nitrogen stream.
  • the low-pressure column also preferably has no top condenser.
  • As reflux liquid in the upper region of the low-pressure column liquid nitrogen from the high-pressure column is used instead.
  • liquid nitrogen from the medium-pressure column it is additionally or alternatively possible to add liquid nitrogen from the medium-pressure column as reflux to the low-pressure column.
  • the invention also relates to a device according to claim 9.
  • the device according to the invention can be supplemented by device features which correspond to the features of the dependent method claims.
  • FIG. 1 atmospheric air is sucked in via line 1 from a main air compressor 2 and compressed to a pressure of about 10 bar.
  • the compressed feed air 3 is cooled in a pre-cooler 4 and then cleaned in a cleaning device 5 containing molecular sieve adsorber, that is freed in particular of water and carbon dioxide.
  • the compressed and purified feed air 6 is divided into three partial streams 10, 20, 30.
  • a first partial flow 10 (direct air flow) is fed without further pressure increase the warm end of a main heat exchanger 8, cooled there to about dew point and fed via lines 11 and 12 of the high pressure column 50 of a distillation column system for nitrogen-oxygen separation, which also has a low pressure column 51 and a main capacitor 53.
  • the main heat exchanger may be formed from a single or multiple parallel and / or serially connected heat exchanger sections, for example one or more plate heat exchanger blocks.
  • the operating pressures in the high-pressure column and the low-pressure column (in each case at the top) are 9.7 bar and approx. 3.0 bar, respectively.
  • the second and the third partial flow 20, 30 are first fed together via line 7 to a first motor-driven booster 9 with aftercooler 15 and there recompressed to an intermediate pressure of about 20 bar.
  • the second partial flow 20 (turbine flow) is further compressed in a turbine-driven secondary compressor 21 with aftercooler 22 to about 28 bar and fed under this pressure via line 23 to the warm end of the main heat exchanger 8.
  • At an intermediate temperature it is withdrawn via line 24, in an expansion turbine 25 working to relax at about high-pressure column pressure and finally introduced via lines 26 and 12 in the high-pressure column.
  • a generator turbine and to eliminate supercharger 21 and aftercooler 22 (not shown).
  • the third partial flow 30 is brought from the intermediate pressure in a second motor-driven booster 31 with aftercooler 32 to a high pressure of 60 bar, passed via line 33 to the main heat exchanger 8 and there cooled and (pseudo-) liquefied. Subsequently, the third partial stream 33 is expanded in an expansion valve 34 to about high pressure column pressure and introduced via line 35 in the distillation column system for nitrogen-oxygen separation, at least partially in liquid form. Alternatively, the relaxation is performed in a turbine 36 which is coupled to a generator 37. A portion 38, 39 of the liquid air may be cooled in a supercooling countercurrent 54 and supplied to the low pressure column 51 at a suitable intermediate point.
  • the gaseous top nitrogen 55 of the high-pressure column 50 is liquefied to a first part 56 in the main condenser 53.
  • a first part 58 of the liquid nitrogen 57 produced in the process is fed as reflux to the high-pressure column 50.
  • a second part 66, 67 is cooled in the subcooling countercurrent 54 and fed to the head of the low pressure column 51 as reflux.
  • a nitrogen-rich intermediate fraction 68, 69 is cooled in the subcooling countercurrent 54 and fed to the low pressure column 51 at an intermediate point.
  • the oxygen-enriched bottoms fraction 70 from the high-pressure column 50 is also cooled in the subcooling countercurrent 54 and fed to a first part 71 of the low-pressure column 51 at another intermediate point.
  • pressurized nitrogen product is recovered under four different pressures.
  • two nitrogen product streams are withdrawn directly from the distillation column nitrogen-oxygen separation system in gas, and heated in the main heat exchanger 8 to about ambient temperature, namely gaseous overhead nitrogen 73, 74, 75 of the low pressure column 51 as low pressure column pressure (GAN) pressurized nitrogen product and a second Part 72, 76 of the top nitrogen 55 of the high pressure column as pressurized nitrogen product under high pressure column pressure (PGAN1).
  • GAN low pressure column pressure
  • PGAN1 pressurized nitrogen product
  • a third part 59 of the liquid nitrogen 57 from the main condenser 53 is fed to a nitrogen internal compression. He will be in one
  • Nitrogen pump 60 brought in the liquid state to an increased nitrogen pressure above the operating pressure of the high pressure column, passed via line 61 to the main heat exchanger 8, there in indirect heat exchange with feed air (pseudo) evaporated and warmed to about ambient temperature and finally under the increased pressure via line 62 as gaseous pressure nitrogen product (ICGAN2) won.
  • a portion 63 of the pumped nitrogen may be throttled in an expansion valve 64 to an intermediate pressure between the high pressure column pressure and the increased nitrogen pressure and recovered under this intermediate pressure as another gaseous pressure nitrogen product 65 (ICGAN1).
  • a pressure oxygen product could be obtained by gaseous removal immediately above the bottom of the low pressure column 51 and then heating in the main heat exchanger at about low pressure column pressure and further compressed in an oxygen compressor if necessary (external compression).
  • it is more favorable here to apply an internal compression by taking an oxygen stream 77 in the liquid state from the lower region of the low-pressure column 51, here directly at the bottom or from the evaporation space of the main condenser 53.
  • the oxygen flow 77 becomes a liquid state Pressure increase to an increased oxygen pressure in an oxygen pump 78 subjected and vaporized in the main heat exchanger 8 in indirect heat exchange with feed air or pseudo-vaporized, wherein a portion of the feed air is liquefied or pseudo-liquefied.
  • At least a first part 80, 81 of the pumped oxygen 79 is thereby obtained as a pressure oxygen product (HP-GOX) under the increased oxygen pressure.
  • Another part 82, 84 of the pumped oxygen 79 can be throttled in an expansion valve 83 to an intermediate pressure between the low-pressure column pressure and the increased oxygen pressure and recovered under this intermediate pressure as another gaseous pressure oxygen product (MP-GOX).
  • a gaseous impure nitrogen stream 85 is taken from the low-pressure column which is less pure than the top nitrogen 73 but contains at least 80% nitrogen. In the embodiment, its nitrogen content is 90%. According to the invention, this stream is used to operate a residual gas column 52, which has a bottom evaporator 85 and is operated at a pressure of 1.4 bar at the top. Of the Impurity stream 85 is introduced into the liquefaction space of the bottom evaporator where it is brought into indirect heat exchange with the bottom liquid of the residual gas column 52 and thereby at least partially condensed. The at least partially liquefied impure nitrogen stream 87 is expanded in a throttle valve 88 to the operating pressure of the residual gas column and introduced into the upper region of the residual gas column 52, in particular directly at the top of the column.
  • a crude liquid oxygen fraction 89 from the high-pressure column 50 is further enriched. It is formed by a portion of the bottom fraction 70, from which it is branched downstream of the subcooling countercurrent 54.
  • the liquid crude oxygen fraction 89 is expanded in an expansion valve 90 and fed to the residual gas column 52 at a first intermediate point.
  • the residual gas column is also fed at a second intermediate point, a partial flow 90 of the liquid air 38 after cooling in the subcooling countercurrent 54.
  • the liquid bottoms fraction 91 of the residual gas column is enriched more strongly with oxygen than the crude oxygen fraction 89 from the high-pressure column 50 and is brought by means of a pump 92 over to the higher pressure of the low-pressure column 51. It is supplied to the low-pressure column via line 93 at a second intermediate point, which is below the first intermediate point at which the impure nitrogen stream 85 is withdrawn. The second intermediate point is also below the feed point of the crude oxygen 71, which is passed directly from the high pressure column 50 in the low pressure column 51.
  • a nitrogen-rich residual stream 94, 95, 96 is withdrawn in gaseous form and in the subcooling countercurrent 54 and in. Main heat exchanger 8 warmed up. If desired, the warm residual gas 96 can still be used as a regeneration gas for the purification unit 5 and / or in an evaporative cooler of the precooling unit 4.
  • FIG. 2 differs from FIG. 1 in that the process also uses a medium pressure column 200 known from three column systems.
  • the medium-pressure column 200 each has a condenser-evaporator as a bottom evaporator 201 and top condenser 202 and is operated under a pressure which is between the operating pressures of low pressure column and high pressure column, in the example at 6 bar.
  • a portion 201 of the sump fraction 70 of the high-pressure column 50 is fed to the medium-pressure column 200 as an insert.
  • a portion 204 of the liquid air 38 can be fed into the medium-pressure column 200.
  • the bottom liquid 205 of the medium-pressure column 200 is partially evaporated in the top condenser 202 of the medium-pressure column 200 and then fed via the lines 206 and 207 at a suitable point in the low-pressure column 51.
  • the gaseous top nitrogen of the medium-pressure column 200 is, as far as it is not condensed in the top condenser 202, passed via line 208 to the main heat exchanger 8 and recovered via line 209 as a further pressure nitrogen product under medium pressure column pressure (PGAN2).
  • this fraction can be analogous to FIG. 1 (Line 93) are fed exclusively or partially into the low-pressure column 51.
  • the feed into the low-pressure column 51 preferably takes place at the same level as the feed of the liquid fraction 207 remaining from the evaporation space of the top condenser 202 of the medium-pressure column.

Landscapes

  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP11006132A 2011-07-26 2011-07-26 Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air Withdrawn EP2551619A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
EP11006132A EP2551619A1 (fr) 2011-07-26 2011-07-26 Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air
CN201210319498.9A CN102901322B (zh) 2011-07-26 2012-07-25 通过低温空气分离获得压力氮和压力氧的方法和装置
US13/558,529 US20130047666A1 (en) 2011-07-26 2012-07-26 Method and device for obtaining pressurized nitrogen and pressurized oxygen by low-temperature separation of air

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
EP11006132A EP2551619A1 (fr) 2011-07-26 2011-07-26 Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air

Publications (1)

Publication Number Publication Date
EP2551619A1 true EP2551619A1 (fr) 2013-01-30

Family

ID=44658528

Family Applications (1)

Application Number Title Priority Date Filing Date
EP11006132A Withdrawn EP2551619A1 (fr) 2011-07-26 2011-07-26 Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air

Country Status (3)

Country Link
US (1) US20130047666A1 (fr)
EP (1) EP2551619A1 (fr)
CN (1) CN102901322B (fr)

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2019533130A (ja) * 2016-08-30 2019-11-14 ８ リバーズ キャピタル，エルエルシー 高圧酸素を生成するための深冷空気分離方法

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN104776685A (zh) * 2014-03-19 2015-07-15 摩尔动力(北京)技术股份有限公司 一种低氧液氮制备方法及其系统
CN105115244B (zh) * 2015-08-10 2017-06-27 开封空分集团有限公司 一种低纯度氧空气分离的装置及方法
US20210140708A1 (en) * 2017-12-28 2021-05-13 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Cryogenic rectification process-based method for producing air product, and air separation system
WO2020083527A1 (fr) * 2018-10-23 2020-04-30 Linde Aktiengesellschaft Procédé et installation de séparation d'air à basse température

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3886758A (en) 1969-09-10 1975-06-03 Air Liquide Processes for the production of nitrogen and oxygen
US5036672A (en) 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
US6227005B1 (en) * 2000-03-01 2001-05-08 Air Products And Chemicals, Inc. Process for the production of oxygen and nitrogen
US6397631B1 (en) * 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
EP1227288A1 (fr) * 2001-01-30 2002-07-31 Linde Aktiengesellschaft Système à trois colonnes pour la séparation cryogénique de l'air
DE102008016355A1 (de) * 2008-03-29 2009-10-01 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Family Cites Families (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5564290A (en) * 1995-09-29 1996-10-15 Praxair Technology, Inc. Cryogenic rectification system with dual phase turboexpansion
US5802873A (en) * 1997-05-08 1998-09-08 Praxair Technology, Inc. Cryogenic rectification system with dual feed air turboexpansion
US5934105A (en) * 1998-03-04 1999-08-10 Praxair Technology, Inc. Cryogenic air separation system for dual pressure feed
DE10113790A1 (de) * 2001-03-21 2002-09-26 Linde Ag Drei-Säulen-System zur Tieftemperatur-Luftzerlegung
US6718795B2 (en) * 2001-12-20 2004-04-13 Air Liquide Process And Construction, Inc. Systems and methods for production of high pressure oxygen
US7143606B2 (en) * 2002-11-01 2006-12-05 L'air Liquide-Societe Anonyme A'directoire Et Conseil De Surveillance Pour L'etide Et L'exploitation Des Procedes Georges Claude Combined air separation natural gas liquefaction plant
BRPI0721930A2 (pt) * 2007-08-10 2014-03-18 Air Liquide Processo e aparelho para a separação de ar por destilação criogênica
JP5417054B2 (ja) * 2009-06-15 2014-02-12 大陽日酸株式会社 空気分離方法及び装置
FR2949846B1 (fr) * 2009-09-10 2012-02-10 Air Liquide Procede et installation de production d'oxygene par distillation d'air
US20110192194A1 (en) * 2010-02-11 2011-08-11 Henry Edward Howard Cryogenic separation method and apparatus
US20120036891A1 (en) * 2010-08-12 2012-02-16 Neil Mark Prosser Air separation method and apparatus
DE102010056560A1 (de) * 2010-08-13 2012-02-16 Linde Aktiengesellschaft Verfahren und Vorrichtung zur Gewinnung von Drucksauerstoff und Druckstickstoff durch Tieftemperaturzerlegung von Luft

Patent Citations (7)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3886758A (en) 1969-09-10 1975-06-03 Air Liquide Processes for the production of nitrogen and oxygen
US5036672A (en) 1989-02-23 1991-08-06 Linde Aktiengesellschaft Process and apparatus for air fractionation by rectification
EP0384483B1 (fr) 1989-02-23 1992-07-22 Linde Aktiengesellschaft Procédé et dispositif de rectification d'air
US6227005B1 (en) * 2000-03-01 2001-05-08 Air Products And Chemicals, Inc. Process for the production of oxygen and nitrogen
EP1227288A1 (fr) * 2001-01-30 2002-07-31 Linde Aktiengesellschaft Système à trois colonnes pour la séparation cryogénique de l'air
US6397631B1 (en) * 2001-06-12 2002-06-04 Air Products And Chemicals, Inc. Air separation process
DE102008016355A1 (de) * 2008-03-29 2009-10-01 Linde Ag Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft

Cited By (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2019533130A (ja) * 2016-08-30 2019-11-14 ８ リバーズ キャピタル，エルエルシー 高圧酸素を生成するための深冷空気分離方法

Also Published As

Publication number Publication date
CN102901322A (zh) 2013-01-30
CN102901322B (zh) 2016-08-10
US20130047666A1 (en) 2013-02-28

Similar Documents

Publication Publication Date Title
EP2235460B1 (fr) Procédé et installation pour la séparation cryogénique d'air
EP1067345B1 (fr) Procédé et dispositif pour la séparation cryogénique des constituants de l'air
EP1994344A1 (fr) Procédé et dispositif de décomposition de l'air à basse température
EP2236964B1 (fr) Procédé et dispositif de séparation de l'air à basse température
EP2015012A2 (fr) Procédé pour la séparation cryogénique d'air
DE10139727A1 (de) Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102007014643A1 (de) Verfahren und Vorrichtung zur Erzeugung von gasförmigem Druckprodukt durch Tieftemperaturzerlegung von Luft
DE102010052545A1 (de) Verfahren und Vorrichtung zur Gewinnung eines gasförmigen Druckprodukts durch Tieftemperaturzerlegung von Luft
DE102009048456A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP1074805B1 (fr) Procédé et dispositif pour la production d'oxygène sous pression
EP2520886A1 (fr) Procédé et dispositif de production d'un produit comprimé à oxygène gazeux par décomposition à basse température d'air
EP3290843A2 (fr) Procédé et dispositif destiné à fabriquer de l'azote pressurisé et liquide par décomposition à basse température de l'air
WO2020169257A1 (fr) Procédé et installation de décomposition d'air à basse température
WO2012019753A2 (fr) Procédé et dispositif permettant d'obtenir de l'oxygène sous pression et de l'azote sous pression par fractionnement cryogénique de l'air
WO2014146779A2 (fr) Procédé et dispositif de production d'azote gazeux sous pression
EP2963369B1 (fr) Procede et dispositif cryogeniques de separation d'air
DE19951521A1 (de) Verfahren und Vorrichtung zur Gewinnung eines Druckprodukts durch Tieftemperaturzerlegung von Luft
EP2551619A1 (fr) Procédé et dispositif destinés à l'obtention d'oxygène pressurisé et d'azote pressurisé par la décomposition à basse température de l'air
EP2053331A1 (fr) Procédé et dispositif de séparation de l'air à basse température
DE102007042462A1 (de) Verfahren und Vorrichtung zur Tieftemperaturzerlegung von Luft
EP2938952A2 (fr) Procédé et dispositif de séparation de l'air à basse température
WO2011110301A2 (fr) Procédé et dispositif de séparation de l'air à basse température
DE19933558C5 (de) Dreisäulenverfahren und -vorrichtung zur Tieftemperaturzerlegung von Luft
WO2017108187A1 (fr) Procédé et dispositif de production d'azote pur et d'oxygène pur par séparation cryogénique d'air
EP2600090B1 (fr) Procédé et dispositif destinés à la production d'oxygène sous pression par décomposition à basse température de l'air

Legal Events

Date Code Title Description
PUAI Public reference made under article 153(3) epc to a published international application that has entered the european phase

Free format text: ORIGINAL CODE: 0009012

AK Designated contracting states

Kind code of ref document: A1

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

AX Request for extension of the european patent

Extension state: BA ME

17P Request for examination filed

Effective date: 20130627

RBV Designated contracting states (corrected)

Designated state(s): AL AT BE BG CH CY CZ DE DK EE ES FI FR GB GR HR HU IE IS IT LI LT LU LV MC MK MT NL NO PL PT RO RS SE SI SK SM TR

STAA Information on the status of an ep patent application or granted ep patent

Free format text: STATUS: THE APPLICATION HAS BEEN WITHDRAWN

18W Application withdrawn

Effective date: 20170202