EP4081747A1 - Procédé et installation pour fournir un produit oxygène - Google Patents

Procédé et installation pour fournir un produit oxygène

Info

Publication number
EP4081747A1
EP4081747A1 EP20812220.0A EP20812220A EP4081747A1 EP 4081747 A1 EP4081747 A1 EP 4081747A1 EP 20812220 A EP20812220 A EP 20812220A EP 4081747 A1 EP4081747 A1 EP 4081747A1
Authority
EP
European Patent Office
Prior art keywords
distillation column
cryogenic liquid
liquid
oxygen product
fed
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.)
Pending
Application number
EP20812220.0A
Other languages
German (de)
English (en)
Inventor
Wolfgang Haag
Daniel Palaniswamy OTTE
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
Publication of EP4081747A1 publication Critical patent/EP4081747A1/fr
Pending legal-status Critical Current

Links

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
    • F25J3/04406—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
    • F25J3/0443—A main column system not otherwise provided, e.g. a modified double column flowsheet
    • 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
    • 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
    • F25J3/04151—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
    • F25J3/0423—Subcooling of liquid process streams
    • 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
    • F25J3/04236—Integration of different exchangers in a single core, so-called integrated cores
    • 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
    • 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
    • F25J3/04321—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 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
    • F25J3/04763—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
    • F25J3/04781—Pressure changing devices, e.g. for compression, expansion, liquid pumping
    • 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
    • F25J2200/90—Details relating to column internals, e.g. structured packing, gas or liquid distribution
    • F25J2200/94—Details relating to the withdrawal point
    • 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
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/50—Oxygen or special cases, e.g. isotope-mixtures or low purity O2
    • F25J2215/56—Ultra high purity oxygen, i.e. generally more than 99,9% O2
    • 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
    • F25J2220/00—Processes or apparatus involving steps for the removal of impurities
    • F25J2220/50—Separating low boiling, i.e. more volatile components from oxygen, e.g. N2, Ar
    • 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
    • F25J2235/04—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams using a pressure accumulator
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
    • F25J2235/50—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2245/00—Processes or apparatus involving steps for recycling of process streams
    • F25J2245/50—Processes or apparatus involving steps for recycling of process streams the recycled stream being oxygen
    • 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
    • F25J2250/02—Bath type boiler-condenser using thermo-siphon effect, e.g. with natural or forced circulation or pool boiling, i.e. core-in-kettle heat exchanger
    • 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
    • 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
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/02—Internal refrigeration with liquid vaporising loop
    • 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
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/62—Details of storing a fluid in a tank

Definitions

  • the present invention relates to a method for providing an oxygen product and a corresponding system according to the respective preambles of the independent claims.
  • distillation column systems can be designed, for example, as one or two-column systems, in particular as classic double-column systems, but also as three-column or multi-column systems.
  • a distillation column system can be used which has a distillation column which is primarily set up to provide nitrogen and which is referred to here as a “nitrogen column”.
  • a corresponding method is also referred to as the SPECTRA method and is explained in more detail below.
  • liquid is removed from the nitrogen column, relaxed, evaporated in a top condenser of the nitrogen column against condensing top gas, which is then partially returned to the nitrogen column as reflux and can partially be removed from the system, then recompressed and returned to the nitrogen column.
  • further liquid from the nitrogen column can also be depressurized, evaporated in the top condenser of the nitrogen column against the condensing top gas of the nitrogen column, depressurized further and removed from the system.
  • an additional column for generating (pure or high-purity) oxygen is provided. This can be fed directly from the nitrogen column or with fluid that has been taken from the nitrogen column and processed further in at least one further distillation column.
  • devices for example distillation columns, for obtaining further air components, in particular the noble gases helium, neon, krypton, xenon and / or argon, can be provided in the above-mentioned distillation column systems.
  • a gaseous, pressurized air product is conventionally formed by removing a cryogenic, liquid air product from the distillation column system used, subjecting it to a pressure increase to a product pressure, and heating it to the gaseous or supercritical state at the product pressure.
  • gaseous, pressurized oxygen of any purity, gaseous, pressurized nitrogen and / or gaseous, pressurized argon can be generated by means of conventional internal compression.
  • the internal compression offers a number of advantages compared to an alternative possible external compression and is explained e.g. by Häring (see above) in Section 2.2.5.2, "Internal Compression".
  • methods and systems for the low-temperature decomposition of air, in which internal compression is used are shown in US 2007/0209389 A1 and in WO 2015/127648 A1.
  • an air product can also be pressurized by means of a partial flow of compressed feed air in a tank arrangement.
  • WO 2014/173496 A2 discloses a method for obtaining oxygen in the sense explained below in an air separation plant, in which a liquid fraction is obtained from feed air and is at least partially used to provide the oxygen.
  • the liquid fraction is temporarily stored in a tank arrangement with at least two tanks, the liquid fraction in at least one of the tanks is supplied and / or withdrawn from at least one of the tanks for providing the air product and is not supplied and withdrawn to any of the tanks at the same time.
  • the composition of the liquid fraction in the tank is determined.
  • EP 3 193 114 A1 discloses a further method with pressure build-up evaporation.
  • the invention proposes a method for providing an oxygen product and a corresponding system according to the respective preambles of the independent claims. Refinements are the subject of the dependent claims and the description below.
  • oxygen should be understood here to mean any liquid or gaseous fluid that contains more than 80% oxygen.
  • oxygen is therefore not limited to pure or high-purity oxygen, but pure or high-purity oxygen can also be provided.
  • highly pure is to be understood as meaning oxygen with a purity of at least 99.9 mol percent. The oxygen is carried out as an oxygen product from a corresponding system, with a "product" no longer being fed back into the system and participating in system-internal cycles.
  • a tank system with a plurality of tanks is used in which a first tank or a first group of the plurality of tanks, but not a second tank or a second group of the plurality of tanks, is filled in a first period of time.
  • the second tank or the second group of tanks, but not the first tank is filled in a second period of time. The same applies to emptying, which can take place at the same time as filling another tank or another group of tanks.
  • the second tank or the second group of tanks but not the first tank or the first group of tanks, and in the first period, the first tank or the first group of tanks but not the second Tank, or the second group of tanks, to be emptied.
  • a “first tank” or a “second tank” is used in each case below, this can, in simplified form, also stand for the first or second group of tanks.
  • Corresponding groups of tanks include tanks operated in parallel, so that in each case at least a first or a second tank (from the first or second group) is operated accordingly.
  • the present invention achieves these advantages by using the blow-off gas, which has hitherto been blown off to the atmosphere, from a pressure build-up system, which can be used in different ways.
  • a pressure build-up system which can be used in different ways.
  • reliquefaction and material use of the oxygen molecules contained in the blow-off gas can take place.
  • the present invention proposes a method for providing an oxygen product using an air separation plant with a distillation column system, in which a cryogenic liquid is removed from the distillation column system, a first portion of the cryogenic liquid being subjected to pressure build-up evaporation by evaporation of a second portion of the cryogenic liquid and the Oxygen product is provided using at least a portion of the first portion of the cryogenic liquid.
  • the pressure build-up evaporation takes place in corresponding tanks from which the first portion of the cryogenic liquid is periodically withdrawn.
  • the second portion of the cryogenic liquid is also at least partially discharged from the tank before the tank is refilled, and the tank is thus released to the starting pressure, which causes the aforementioned blow -Off gas is provided.
  • the cryogenic liquid can be formed at 1 to 4 bara, for example approx. 3 bara, in particular in a pure oxygen column of a SPECTRA process, as also indicated again below, and transferred via a gradient into tanks which are in the Pressure build-up evaporation can be used.
  • the pressure build-up evaporation provides a pressure of, for example, approx. 8 to 16 bara or higher. After filling up, the second portion of the cryogenic liquid is usually not used any further.
  • the present invention now proposes that at least part of the vaporized second portion of the cryogenic liquid is used for providing the oxygen product. In this way, the advantages already mentioned can be achieved.
  • the correspondingly evaporated cryogenic liquid is at least not completely lost in the process.
  • the use can in particular comprise a material use and / or a thermal use and / or a pressure use.
  • Material use is in particular when the oxygen molecules contained in the second portion are converted into the ultimately liquid oxygen product, in particular by liquefaction and, if necessary, feeding into a column used to form the oxygen product or directly to the oxygen product.
  • a thermal use can exist in particular when the second portion is used as a cooling or heating medium, for example in a sump evaporator (sump reboiler) of a rectification column or for cooling another material flow, for example nitrogen.
  • thermal use can also exist when the second component is relaxed and in this way "cold" is produced or heat is dissipated.
  • expansion devices such as turbines, which can for example be coupled with brakes of any type.
  • pressure can in particular include the expansion of a corresponding material flow in an expansion turbine which is coupled either to a generator or to a booster for compressing a further flow.
  • a particularly preferred embodiment of the invention comprises directing the corresponding gas back into the air separation plant and liquefying it in a sump reboiler of a distillation column in which the cryogenic liquid is formed. Then the liquid obtained in this way becomes the cryogenic liquid in the Distillation column (or the cryogenic liquid removed from the distillation column) and fed back into the pressure build-up evaporation. In this way, the net amount of liquid oxygen to be produced can be reduced or, in total, more liquid oxygen can be produced. Further details are explained below for a corresponding embodiment.
  • a SPECTRA process is characterized in that the distillation column system comprises a first distillation column, liquid being removed from the first distillation column, expanded and evaporated against condensing overhead gas of the first distillation column, which is at least partially returned to the first distillation column , wherein the vaporized liquid is at least partially recompressed and fed back into the first distillation column.
  • further liquid can also be removed from the first distillation column, expanded, evaporated against the condensing top gas of the first distillation column, and at least partially discharged from the air separation plant.
  • the distillation column system can, for example, comprise a second distillation column fed from the first distillation column, the second distillation column being operated using a sump reboiler and the cryogenic liquid being removed from the second distillation column.
  • the present invention can also include any variants thereof in which, for example, an additional high-purity oxygen column is used, and / or systems with argon recovery, in which one of the columns used is withdrawn from a side stream and transferred to an argon column or a column system for argon generation.
  • the cryogenic liquid can be taken from any further distillation column which is connected downstream of the first distillation column, i.e.
  • the cryogenic liquid can be withdrawn, in particular, in the form of high-purity oxygen from a further distillation column, which is not the mentioned second distillation column but is connected downstream of it.
  • the vaporized second portion of the cryogenic liquid, or the portion thereof which is fed to further use to provide the oxygen product can in particular be at least partially fed into the second distillation column.
  • liquefaction takes place before the feed, so that the oxygen in the gas can be used completely as a material, as explained below.
  • gaseous feeding into a corresponding distillation column and liquefaction there can also take place.
  • a particularly preferred embodiment of the invention comprises, as already mentioned in principle, that the vaporized second portion of the cryogenic liquid, or the portion thereof which is further used to provide the oxygen product, is at least partially cooled in the sump reboiler of the second distillation column.
  • the minimum pressure of the liquid oxygen in the sump reboiler is approx. 300 mbar above the pressure in the sump of the distillation column. Due to further line and valve pressure losses on the way from the tanks in the pressure build-up evaporation to the sump reboiler, the minimum pressure of the gas is limited to a value of approx. 500 or at least 400 mbar above the column sump. This means that the second part, when relaxing from, for example, 11 bara to a corresponding pressure value can be made usable. The gas at a lower pressure level must therefore continue to be blown off into the atmosphere.
  • the vaporized second portion of the cryogenic liquid, or the portion thereof which is fed to further use to provide the oxygen product can be at least partially cooled in a further heat exchanger of the air separation plant.
  • the further heat exchanger can in particular be a heat exchanger which is supercooled liquid nitrogen, which is formed from top gas of the first distillation column, in order to provide a liquid nitrogen product. In this way, liquefied oxygen can be fed into the cryogenic liquid.
  • a sump reboiler is used in a second distillation column of the type described, the minimum pressure here can be reduced to a value of approx. 200 mbar above the pressure in the sump of the distillation column plus the heat exchanger pressure loss. This corresponds to the line and valve pressure losses.
  • the energy saving for the case study mentioned above is 101 kW (1.4%).
  • the present invention can be implemented with minimal intervention in the overall system of the air separation plant.
  • the second portion for transferring heat to it is also at least partially passed through a heat exchanger and is heated in the process. This can also be done in a separate heat exchanger or in the main heat exchanger.
  • the second portion can be heated separately (ie without being mixed with further fluid) or together with further fluid, for example residual gas from the air separation plant or another fluid, which in particular can be present at a lower pressure level than the second portion.
  • the present invention is particularly suitable for processes for the production of cryogenic liquid and an oxygen product with an oxygen content of more than 99 mol percent, in particular more than 99.5 or 99.9 mol percent.
  • a tank system with one or more alternately filled and emptied tanks is advantageously used, with the filled tank being pressurized by evaporation of the second portion of the cryogenic liquid and the second portion the cryogenic liquid is discharged from the respective empty tank.
  • This operation results in a surge-like or pulsating accumulation of the second portion of the cryogenic liquid, that is to say of the liquefying gas.
  • This can therefore advantageously be temporarily stored at least temporarily, in particular in a buffer tank.
  • the present invention also extends to an air separation plant, with respect to which reference is expressly made to the corresponding independent patent claim.
  • a corresponding air separation plant which is preferably set up to carry out a method, as was previously explained in different configurations, benefits in the same way from the advantages already mentioned above.
  • Figure 1 illustrates an air separation plant according to an embodiment of the present invention in a simplified representation.
  • FIG. 2 illustrates an air separation plant according to an embodiment of the present invention in a simplified partial representation.
  • FIG. 3 illustrates an air separation plant according to an embodiment of the present invention in a simplified partial representation.
  • FIG. 4 illustrates an air separation plant according to an embodiment of the present invention in a simplified partial representation.
  • FIG. 5 illustrates a pressure build-up evaporation for an air separation plant according to an embodiment of the present invention.
  • FIG. 1 an air separation plant according to an embodiment of the present invention is shown in the form of a schematic process flow diagram and denoted as a whole by 100.
  • the air separation plant 100 is supplied with air in the form of a feed air stream a via a filter 1 from the atmosphere A, compressed in a main air compressor 2, cooled with water W in an aftercooler and a direct contact cooler (not specifically designated), dried in an adsorber station 4 and freed from carbon dioxide, fed to a main heat exchanger 5 on the warm side, guided in the main heat exchanger 5 almost to the cold end, and fed into a first distillation column 11 of a distillation column system 10.
  • the feed takes place partly without further cooling in the form of a stream a1, partly after cooling in a sump reboiler 121 in the sump of a second distillation column 12 of the distillation column system 10.
  • the air separation plant 100 is designed to carry out a SPECTRA process, including two liquid streams b and c at different positions, ie via a side take-off and from the sump, taken from the first distillation column 11, each subcooled in the main heat exchanger 5, expanded and in a heat exchanger 111 evaporated against condensing head gas of the first distillation column 11.
  • Liquid nitrogen can be fed in from a store I, for example.
  • the stream b is then at least partially in one with a Expansion machine 7 and a compressor 6 coupled to a brake, which is not separately designated, recompressed, cooled again in the main heat exchanger 5, and fed back into the first distillation column 11.
  • the material flow c is at least partially heated in the main heat exchanger 5, expanded in the expansion machine 7 and discharged from the air separation plant 100.
  • the top gas is removed from the first column 11 in the form of a stream c, which is then divided into a substream c1, which is passed into the heat exchanger 111 and liquefied there, and a substream c2, which is discharged from the air separation plant 100 as product N1, N2, divided up.
  • a substream c1 which is passed into the heat exchanger 111 and liquefied there, and a substream c2, which is discharged from the air separation plant 100 as product N1, N2, divided up.
  • some of the stream c1 is returned to the first column 11 as reflux.
  • a further portion can be cooled against a portion of itself in a heat exchanger 8 and discharged as liquid nitrogen product C.
  • a portion can be discharged from the air separation plant 100 as a purge stream P.
  • the second distillation column 12 is fed with a liquid side stream d from the first distillation column 11, which is supercooled in the bottom reboiler 121 and then fed to the top of the second distillation column 12.
  • An oxygen product is formed by cryogenic, oxygen-rich liquid which is taken from the bottom of the second distillation column 12 in the form of a stream e.
  • the material flow e is fed as liquid oxygen to a pressure build-up evaporation 20 (see for the details below and link E in FIG. 1).
  • Impure nitrogen is withdrawn from the top of the second distillation column in the form of a stream f and, after combining, among other things, heated with the relaxed stream c in the main heat exchanger 5 and released into atmosphere A and / or used as a regeneration gas in adsorber station 4.
  • a further treatment of the liquid oxygen of the material flow e takes place in the greatly simplified illustrated pressure build-up evaporation 20.
  • Liquid oxygen which has been pressurized in the pressure build-up evaporation 20, is diverted in the form of a material flow g to an extraction point G. It is also possible to subject this liquid oxygen, as illustrated by K, to evaporation in the main heat exchanger 5 and from the To divert air separation unit 100. Gas accumulating during the pressure build-up evaporation is either released to the atmosphere, as illustrated here by V, but in an embodiment of the invention shown here, it is partly passed through the sump reboiler 121 and fed into the material flow e. In this way, material use takes place. Heat integration in the main heat exchanger 5 can also take place, as illustrated by K.
  • FIGS. 2, 3 and 4 each illustrate part of an air separation plant according to an embodiment of the invention, which, in addition to the components shown, can have, for example, those of the air separation plant 100 according to FIG.
  • the integration can be seen from the illustrated material flows, including the material flows a2, d, e and f.
  • a buffer memory 21 is provided in each case. This is able to buffer the periodically occurring gas quantities from the pressure build-up evaporation 20, as explained in relation to FIG. 5, in order to continuously feed them into use.
  • the material flow h is used essentially as in the air separation plant 100 according to FIG. 1, this is not the case in the embodiment according to FIG. 3.
  • the stream h is fed directly into the second distillation column 12.
  • thermal use is also possible in the heat exchanger 8, which in FIG. 4 is denoted by 8 'for the sake of better differentiation and is equipped with corresponding additional passages.
  • the material flow h which is also designated by h 'downstream of the heat exchanger 8' for the sake of better distinguishability, can then in particular be fed to the material flow e.
  • FIGS. 1 to 4 can also be combined. For example, operation with or without a buffer store 21 and with or without thermal utilization in a heat exchanger 8 'can take place in all cases.
  • the types of use illustrated in FIGS. 1 to 4 can each also include only the use of substreams of the material flow h, with further substreams being able to be used for other purposes.
  • FIG. 5 illustrates a pressure build-up evaporation 20 for an air separation plant according to an embodiment of the present invention in FIG schematic representation.
  • the pressure build-up evaporation is also denoted here by 20.
  • the pressure build-up evaporation 20 can in particular correspond to the pressure build-up evaporation described in EP 3 193 114 A1, but can also deviate therefrom.
  • use of gas that is formed in a pressure build-up evaporation is provided. This gas is obtained in particular after the tank has been emptied, ie after a tank that is pressurized in the pressure build-up evaporation has been emptied during the subsequent expansion for refilling.
  • the present invention is therefore suitable for all cases of pressure build-up evaporation in which tanks are emptied accordingly.
  • An essential component of the pressure build-up evaporation 20 is a double tank system, which is designated here as a whole by 70, and which has two tanks 71 and 72.
  • a pump 55 By means of a pump 55, the cryogenic liquid of the fluid flow e, here denoted by 41, can be increased in pressure.
  • the pump 55 is not absolutely necessary if the pressure build-up through evaporation alone is sufficient.
  • the pump 55 is regularly omitted and the cryogenic liquid of the stream 41 is fed into the tanks 71 and 72 at the distillation pressure in the second distillation column 12.
  • the tank system 70 is equipped with a pressure build-up evaporation device 75.
  • a liquid portion of the cryogenic liquid of the stream 41 taken from the tanks 71 or 72 is evaporated.
  • the vaporized gas which is present under an increased pressure, is fed to a head space of the tanks 71 and 72, respectively.
  • the pump 55 can be saved and only pressure build-up evaporation can be used.
  • part of the product is converted into the gas phase. If the cryogenic liquid is removed from the respective tank 71, 72, the gas phase remains. This is vented to the atmosphere in conventional processes, as illustrated here and before with V. Instead, the embodiment of the invention illustrated here provides for a part in the form of the material flow h to be used as explained above.
  • the pressurized fluid stream 41 is fed to either the tank 71 or the tank 72 and then pressurized.
  • the tanks 71 and 72 become alternative each other charged with the cryogenic liquid of the fluid flow 41, ie during a first period the cryogenic liquid of the fluid flow 41 is fed to the first tank 71 and not to the second tank 72 and during a second period to the second tank 72 and not to the first tank 71.
  • a tank control 80 for example, can be provided for controlling correspondingly inserted valves 71a and 72a.
  • cryogenic liquid is always removed from that of the tanks 71, 72 to which no cryogenic liquid of the fluid flow 41 is currently being fed. This liquid can generally be discharged directly after the removal.
  • this is transferred unheated to a further tank 73.
  • a further tank 73 when the further tank 73 is completely filled, provision can also be made, as illustrated here by means of a line 74, to pass the corresponding fluid directly on and to heat it.
  • the fluid can be heated, for example, in a main heat exchanger 5 of a corresponding air separation plant, for example the air separation plant 100 according to FIG. 1, and / or in an additional evaporator 90.
  • the cryogenic liquid can, however, also be removed from the further tank 73 in the liquid state and stored in liquid form in a storage tank 76 until it is used. Further withdrawals upstream and / or downstream of the further tank 73 are also possible in principle.

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Abstract

La présente invention concerne un procédé permettant de fournir un produit oxygène au moyen d'une installation de séparation d'air (100) comportant un système de colonne de distillation (10), selon lequel un liquide très froid est prélevé du système de colonne de distillation (10), une première fraction du liquide très froid étant soumise à une vaporisation par montée de pression par vaporisation d'une seconde fraction du liquide très froid et le produit oxygène étant obtenu au moyen d'au moins une partie de la première fraction du liquide très froid. Selon l'invention, après l'élévation de la pression, au moins une partie de la seconde fraction vaporisée du liquide très froid est acheminée pour une nouvelle utilisation afin de fournir le produit oxygène. La présente invention concerne également une installation de séparation d'air (100) correspondante.
EP20812220.0A 2019-12-23 2020-11-19 Procédé et installation pour fournir un produit oxygène Pending EP4081747A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP19020722 2019-12-23
PCT/EP2020/025522 WO2021129948A1 (fr) 2019-12-23 2020-11-19 Procédé et installation pour fournir un produit oxygène

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EP4081747A1 true EP4081747A1 (fr) 2022-11-02

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EP (1) EP4081747A1 (fr)
CN (1) CN114846287A (fr)
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WO2023165736A1 (fr) 2022-03-01 2023-09-07 Linde Gmbh Procédé et installation pour fournir de l'oxygène gazeux sous pression

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Publication number Priority date Publication date Assignee Title
DE676616C (de) 1936-09-04 1939-06-08 Messer & Co Gmbh Verfahren zur Erzeugung von unter Druck stehendem gasfoermigem Sauerstoff
US2772545A (en) * 1952-05-13 1956-12-04 Air Prod Inc Liquefied gas pressurizing systems
DE2238866B1 (de) * 1972-08-07 1973-10-11 Linde Ag, 6200 Wiesbaden Verfahren und Vorrichtung zum Um walzen der Flüssigkeit in einem Ver dämpfer Kondensator einer Tieftemperatur Gaszerlegungsanlage
US5148680A (en) 1990-06-27 1992-09-22 Union Carbide Industrial Gases Technology Corporation Cryogenic air separation system with dual product side condenser
US6295840B1 (en) 2000-11-15 2001-10-02 Air Products And Chemicals, Inc. Pressurized liquid cryogen process
US7533540B2 (en) 2006-03-10 2009-05-19 Praxair Technology, Inc. Cryogenic air separation system for enhanced liquid production
EP2989400B1 (fr) 2013-04-25 2021-12-29 Linde GmbH Procédé permettant d'obtenir un produit air dans une installation de séparation de l'air à stockage temporaire et installation de séparation de l'air
WO2015127648A1 (fr) 2014-02-28 2015-09-03 Praxair Technology, Inc. Distribution de courant de produit sous pression
EP3193114B1 (fr) 2016-01-14 2019-08-21 Linde Aktiengesellschaft Procédé de production d'un produit d'air dans une installation de séparation d'air et installation de séparation d'air
JP6900241B2 (ja) * 2017-05-31 2021-07-07 レール・リキード−ソシエテ・アノニム・プール・レテュード・エ・レクスプロワタシオン・デ・プロセデ・ジョルジュ・クロード ガス製造システム

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