EP3864357B1 - Procédé de production d'un ou d'une pluralité de produits gonflables et installation de séparation de l'air - Google Patents

Procédé de production d'un ou d'une pluralité de produits gonflables et installation de séparation de l'air

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Publication number
EP3864357B1
EP3864357B1 EP19797562.6A EP19797562A EP3864357B1 EP 3864357 B1 EP3864357 B1 EP 3864357B1 EP 19797562 A EP19797562 A EP 19797562A EP 3864357 B1 EP3864357 B1 EP 3864357B1
Authority
EP
European Patent Office
Prior art keywords
time
period
air
operating period
pressure
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.)
Active
Application number
EP19797562.6A
Other languages
German (de)
English (en)
Other versions
EP3864357A1 (fr
EP3864357C0 (fr
Inventor
Dirk Schwenk
Dimitri GOLUBEV
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
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Publication date
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Publication of EP3864357A1 publication Critical patent/EP3864357A1/fr
Application granted granted Critical
Publication of EP3864357B1 publication Critical patent/EP3864357B1/fr
Publication of EP3864357C0 publication Critical patent/EP3864357C0/fr
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Anticipated expiration legal-status Critical

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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
    • F25J3/04012—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling
    • F25J3/04018—Providing pressurised feed air or process streams within or from the air fractionation unit by compression of warm gaseous streams; details of intake or interstage cooling of main feed air
    • 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
    • F25J3/04193—Division of the main heat exchange line in consecutive sections having different functions
    • F25J3/04206—Division of the main heat exchange line in consecutive sections having different functions including a so-called "auxiliary vaporiser" for vaporising and producing a gaseous product
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04248—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion
    • F25J3/04284—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/0429—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using internal refrigeration by open-loop gas work expansion, e.g. of intermediate or oxygen enriched (waste-)streams of feed air, e.g. used as waste or product air or expanded into an auxiliary column
    • F25J3/04303—Lachmann expansion, i.e. expanded into oxygen producing or low pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04478—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures
    • F25J3/0449—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for controlling purposes, e.g. start-up or back-up procedures for rapid load change of the air fractionation unit
    • 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
    • F25J3/04472—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages
    • F25J3/04496—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 the cold from cryogenic liquids produced within the air fractionation unit and stored in internal or intermediate storages for compensating variable air feed or variable product demand by alternating between periods of liquid storage and liquid assist
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/0483—Rapid load change of the air fractionation unit
    • 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
    • F25J3/04812—Different modes, i.e. "runs" of operation
    • F25J3/04836—Variable air feed, i.e. "load" or product demand during specified periods, e.g. during periods with high respectively low power costs
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/40—One fluid being air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2250/00—Details related to the use of reboiler-condensers
    • F25J2250/30—External or auxiliary boiler-condenser in general, e.g. without a specified fluid or one fluid is not a primary air component or an intermediate fluid
    • F25J2250/50—One fluid being oxygen
    • 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 invention relates to a process for obtaining one or more air products and a corresponding air separation plant according to the respective preambles of the independent patent claims.
  • Air separation plants have rectification column systems, which can be designed, for example, as two-column systems, in particular as classic Linde double-column systems, but also as three- or multi-column systems.
  • rectification columns for the extraction of nitrogen and/or oxygen in the liquid and/or gaseous state i.e., the rectification columns for nitrogen-oxygen separation
  • rectification columns for the extraction of other air components in particular the noble gases krypton, xenon, and/or argon.
  • air separation plants with corresponding rectification columns can also be the subject of the present invention at any time.
  • the rectification columns of the rectification column systems mentioned are operated at different pressure levels.
  • Double column systems have a so-called high-pressure column (also referred to as pressure column, medium-pressure column or lower column) and a so-called low-pressure column (also referred to as upper column).
  • the pressure level of the high-pressure column is, for example, 4.7 to 6.7 bar, preferably about 5.5 bar.
  • the low-pressure column is operated at a pressure level of, for example, 1.3 to 1.8 bar, preferably about 1.4 bar.
  • the pressure levels specified here and below are absolute pressures. at the top of the respective columns. The values given are merely examples and can be changed if necessary.
  • the US 4 251 248 A discloses a method and apparatus for automatically changing operating sequences in an air separation plant to increase or decrease product quantities. Intended change values, including for feed air, are calculated from the values of the correspondingly increased or decreased product quantities.
  • Purities of air products are kept substantially constant during fluctuations in the demand for one of the products or in the quantity or pressure of feed air by introducing an excess of nitrogen-rich liquid into the rectification column system when the demand for the product or the quantity of feed air increases and by withdrawing and storing an excess of nitrogen-rich liquid from the distillation apparatus when the demand for the product or the quantity of feed air decreases.
  • a cryogenic air separation plant subject to periods of significant changes in product demand is subject to US 6 006 546 A .
  • the system is specifically controlled during these periods to minimize the effects of transient operation on product purity.
  • Rapid changes in oxygen demand and operating air pressure are handled according to the US 5 224 336 A compensated by a net transfer of cold in the form of liquid nitrogen into and out of the distillation system. This cold transfer is accomplished using a liquid nitrogen reservoir connected to the distillation system's reflux path.
  • the present invention aims to make the extraction of air products using air separation plants more flexible and to enable overall faster load changes.
  • Main compressor/booster compressor processes are characterized by the fact that only a portion of the total feed air volume supplied to the rectification column system is compressed to a pressure level that is significantly higher than the pressure level of the high-pressure column, i.e., by at least 3, 4, 5, 6, 7, 8, 9, or 10 bar. A further portion of the feed air volume is compressed only to the pressure level of the high-pressure column or to a pressure level that differs from the pressure level of the high-pressure column by no more than 1 to 2 bar, and is fed into the high-pressure column at this lower pressure level.
  • An example of a main compressor/booster compressor process is shown in Figure 2.3A by Häring (see above).
  • the total amount of feed air supplied to the rectification column system is compressed to a pressure level that is significantly higher, i.e., at least 3, 4, 5, 6, 7, 8, 9 or 10 bar, than the pressure level of the high-pressure column.
  • the pressure difference can be up to 14, 16, 18 or 20 bar, for example.
  • High-pressure processes are known, for example, from the EP 2 980 514 A1 and the EP 2 963 367 A1 known.
  • the present invention can be used in air separation plants with so-called internal compression (IV, IC), but also in air separation plants with external compression.
  • internal compression at least one product provided by the air separation plant is formed by withdrawing a cryogenic liquid from the rectification column system, subjecting it to a pressure increase in the liquid state, and, depending on the prevailing pressure, converting it into either a gaseous or supercritical state by heating.
  • internal compression can be used to produce internally compressed gaseous oxygen (GOX IV, GOX IC), internally compressed gaseous nitrogen (GAN IV, GAN IC), or internally compressed gaseous argon (GAR IV, GAR IC).
  • Internal compression offers a number of technical advantages over external compression of corresponding products, which is also possible in principle, and is explained in the specialist literature, for example in Häring (see above), Section 2.2.5.2, "Internal Compression.”
  • liquids and gases may be rich or poor in one or more components, where "rich” may mean a content of at least 90%, 95%, 99%, 99.5%, 99.9% or 99.99% and “poor” may mean a content of at most 10%, 5%, 1%, 0.1% or 0.01% on a mole, weight or volume basis.
  • liquids and gases can be enriched or depleted in one or more components. These terms refer to a content in a starting liquid or gas from which the liquid or gas in question was obtained.
  • the liquid or gas is "enriched” if it contains at least 1.1 times, 1.5 times, 2 times, 5 times, 10 times, 100 times, or 1,000 times the content of a corresponding component, and "depleted” if it contains at most 0.9 times, 0.5 times, 0.1 times, 0.01 times, or 0.001 times the content of the starting liquid or gas.
  • oxygen is mentioned here, this also includes a liquid or gas that is rich in oxygen, but need not consist exclusively of it.
  • the present invention proposes a process for obtaining one or more air products according to independent process claim 1, in which an air separation plant with a rectification column system is used, in which compressed air is processed in an adjustable total air quantity.
  • a load change is carried out in a third operating period from a first point in time to a second point in time.
  • the second operating period lies after the first operating period and the third operating period between the first operating period and the second operating period. Without further measures this can, as mentioned, lead to the disadvantageous effects explained.
  • a load change can represent an increase or decrease in load, depending on whether the first total air volume is lower or higher than the second total air volume.
  • the first, second and third operating periods represent operating periods that do not overlap in time, and the third operating period always lies between the first and second or the second and first operating periods. This does not exclude the existence of further operating periods.
  • an adjustment of a quantity of a liquid which is formed by rectification using the compressed air and is transported in or out of the rectification column system is changed from a third point in time to a fourth point in time, wherein the third point in time is before or after the first point in time and before the second point in time, and the fourth point in time is after the first point in time and the third point in time and before or after the second point in time.
  • the first, the second, the third and fourth points in time are each within the third operating period, but wherein, for example, the third before the first point in time and the fourth after the second point in time, i.e. the third operating period does not have to start at the first point in time and end at the second point in time.
  • the third operating period can be between the earliest point in time and the latest point in time of these points in time, but can also extend over a longer period.
  • a period between the first point in time and the second point in time is set in such a way that it differs by no more than 20%, 10%, 5% or 1% from a period between the third point in time and the fourth point in time.
  • the said periods can also be set to be the same or essentially the same.
  • the setting can be made in particular by using corresponding setpoints or default values in a regulation or control system.
  • a change in the amount of fluid formed by rectification using compressed air and transported into or out of the rectification column system is proposed that is not synchronous with the change in the total air quantity.
  • This change is carried out in particular by a corresponding setpoint specification of a control or regulating system of an air separation plant and is carried out by suitable actuators, in particular valves, slides and the like.
  • Such control or regulating can be carried out in particular on the basis of recorded actual values and can comprise all measures known from the field of control or regulating technology, insofar as they are suitable and expedient for use in the present invention.
  • the variation of the amount of fluid produced by rectification using compressed air and transported into or out of the rectification column system can be achieved, in particular, by using a corresponding setpoint specification.
  • a corresponding controller output is additionally adjusted (typically within a range of no more than ⁇ 5%) by a trim controller. In extreme cases, this can result in an actual value at the end of the adjustment differing slightly from a given setpoint (but no more than 5%).
  • the present invention can be used in particular in air separation plants whose rectification column system has a high-pressure column operated at a first pressure level and a low-pressure column operated at a second pressure level below the first pressure level, wherein the liquid, the amount of which is changed in the third operating period, as mentioned, is a portion of a gaseous, nitrogen-rich overhead product of the high-pressure column, which is liquefied and fed as reflux to the low-pressure column.
  • the present invention can be used in particular in an air separation plant with a secondary condenser for heating an internally compressed oxygen product. In a corresponding air separation plant, internal or external compression of air products can be carried out, and process engineering interconnections with nitrogen and air circuits can be used. Air separation plants with multiple high-pressure columns can also be used.
  • a period between the first time and the second time is adjusted by changing the first time and/or the second time.
  • a delay time provided within the scope of the present invention is adapted to this change, i.e. if a period of time between the first time and the third time is set as a function of the setting of the period between the first time and the second time by changing the third time.
  • the third time is after the first time and the fourth time is after the second time, the period between the first time and the third time is extended; if the period between the first time and the second time is shortened, the period between the first time and the second time is extended.
  • a longer delay time is selected when the load change speed increases.
  • the present invention also extends to an air separation plant, according to independent device claim 11, which is designed to obtain one or more air products and has a rectification column system, wherein the air separation plant is designed to process compressed air in an adjustable total air quantity in the rectification column system and, in doing so, to set the total air quantity to a first value during a first operating period and to a second value different from the first value during a second operating period, and to change the setting of the total air quantity in a third operating period from a first time point to a second time point from the first value to the second value.
  • the second operating period lies after the first operating period
  • the third operating period lies between the first operating period and the second operating period.
  • the air separation plant is equipped with a control unit that is programmed to change, in the third operating period, a setting of a quantity of a liquid that is formed by rectification using the compressed air and transported into or out of the rectification column system, from a third point in time to a fourth point in time, wherein the third point in time is before or after the first point in time and before the second point in time, and the fourth point in time is after the first point in time and the third point in time and before or after the second point in time. It is further configured to set a period between the first point in time and the second point in time such that it differs from a period between the third point in time and the fourth point in time by no more than 20% or another of the aforementioned difference values.
  • control unit is programmed to carry out a method according to independent method claim 1, and in particular is programmed to carry out a method as previously explained in different embodiments.
  • An air separation plant provided according to the invention is particularly designed to carry out corresponding processes and has specifically designed means for this purpose.
  • FIG. 1 An air separation plant that can be operated according to an embodiment of the invention is illustrated in the form of a simplified process flow diagram and is designated overall by 100.
  • the air separation plant 100 has a distillation column system 10 comprising a high-pressure column 11 and a low-pressure column 12.
  • feed air (A) is drawn in and compressed by a main air compressor 1 through a filter 2.
  • a correspondingly formed compressed air stream a is precooled and purified in a generally known manner in a precooling device 3 operated with cooling water (B) and a purification device 4.
  • Air from the precooled and purified compressed air stream a is fed to a main heat exchanger 5 in the form of two partial streams b and c on the warm side.
  • Partial flow b is taken from the main heat exchanger 5 at an intermediate temperature level and expanded (blown) into the low-pressure column 12 by means of an injection turbine 6, which may be coupled to an oil brake (not specifically designated) or a generator.
  • Partial flow c is taken from the cold side of the main heat exchanger 5, passed through a secondary condenser 7, and fed into the high-pressure column 11 via a valve (not specifically designated).
  • an oxygen-enriched liquid bottom product and a nitrogen-enriched or nitrogen-rich gaseous top product are formed.
  • the bottom product of the high-pressure column 11 is passed through a subcooling countercurrent column 8 in the form of a stream d and fed into the low-pressure column 12.
  • the top product of the high-pressure column 11 is partly liquefied in the form of a stream e in a main condenser 13 that connects the high-pressure column 11 and the low-pressure column 12 in a heat-exchanging manner, and partly heated in the form of a stream f in the main heat exchanger 5 and discharged from the plant as a gaseous pressurized nitrogen product.
  • An oxygen-rich liquid bottom product is formed in the low-pressure column 12 and, in the form of a stream k, is pressure-increased in the liquid state in an internal compression pump 9. At least a portion of this can be fed to the secondary condenser 7 in the form of a stream I and heated there. If required, a further portion can be fed back into the low-pressure column 12 in the form of a stream m via a valve (not specifically designated).
  • the material stream I is at least largely evaporated.
  • a correspondingly evaporated material stream n is heated in the main heat exchanger 5, converted from the liquid to the gaseous or supercritical state, and discharged from the air separation plant 100 as a gaseous pressurized oxygen product (C).
  • a fill level in a liquid tank of the secondary condenser 7 is regulated by the feed stream I. If necessary, liquid can be released to the atmosphere (D) in the form of a material stream o.
  • the sump of the high-pressure column 11 essentially remains as a possible liquid storage facility for load changes.
  • overhead gas is withdrawn from the top of the low-pressure column 12 in the form of a stream p and is partly passed through the subcooling counterflow 8 and the main heat exchanger 5 in the form of a stream q, where it is heated.
  • impure nitrogen which is withdrawn from the low-pressure column 12 in the form of a stream r.
  • the latter streams can be used in various ways in the air separation plant 100, provided as a product, and/or released to the atmosphere (D).
  • the tank 20 can be used, in particular, to buffer a return flow to the low-pressure column 12.
  • a corresponding supplement can be made by means of a stream s from the tank 20, and if the amount of such a nitrogen-rich liquid exceeds the product demand or the demand in the air separation plant 100, it can be fed into the tank 20.
  • a third operating period T3 is therefore provided here.
  • the amount of air 101 fed into the distillation column system and processed there is changed from the first value to the second value from a first time X1 to a second time X2.
  • a setting of a quantity of a fluid that is formed using the compressed air by rectification and transported in or out of the rectification column system here namely the gaseous nitrogen-rich overhead product of the high-pressure column, which is liquefied and fed to the low-pressure column as reflux according to the specification 102, is changed with a delay compared to the fed-in and processed air quantity 101, specifically here from a third time X3 and up to a fourth time X4.
  • the third time X3 here is after the first time X1 and before the second time X2, and the fourth time X4 is after the first time X1 and the third time X3 and after the second time X2.
  • the representation according to Figure 4 corresponds to the representation according to Figure 3 over an extended period of time.
  • "purge" oxygen 107 is periodically vented to the atmosphere (see stream o in Figure 1 ) to prevent the accumulation of undesirable components. In principle, this can also be injected into the compressed oxygen product (C).

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Claims (12)

  1. Procédé permettant l'obtention d'un ou de plusieurs produits formés à partir d'air, dans lequel une installation de séparation d'air (100) comportant un système à colonne de rectification (10) est utilisée, dans lequel de l'air comprimé est traité dans une quantité d'air totale réglable, dans lequel la quantité d'air totale est réglée sur une première valeur pendant une première période de fonctionnement (T1) et sur une deuxième valeur différente de la première valeur pendant une deuxième période de fonctionnement (T2), dans lequel le réglage de la quantité d'air totale est modifié de la première valeur à la deuxième valeur pendant une troisième période de fonctionnement (T3) à partir d'un premier moment (X1) et jusqu'à un deuxième moment (X2), et dans lequel la deuxième période de fonctionnement (T2) se situe après la première période de fonctionnement (T1) et la troisième période de fonctionnement (T3) se situe entre la première période de fonctionnement (T1) et la deuxième période de fonctionnement (T2), dans lequel, pendant la troisième période de fonctionnement (T3), un réglage d'une quantité d'un liquide formé par rectification à l'aide de l'air comprimé et transporté dans le système à colonne de rectification (10) ou hors de celui-ci est modifié à partir d'un troisième moment (X3) et jusqu'à un quatrième moment (X4), dans lequel le troisième moment (X3) se situe avant ou après le premier moment (X1) et avant le deuxième moment (X2) et le quatrième moment (X4) se situe après le premier moment (X1) et le troisième moment (X3) et avant ou après le deuxième moment (X2), une période entre le premier moment (X1) et le deuxième moment (X2) est réglée de telle sorte qu'elle ne diffère pas de plus de 20 % d'une période entre le troisième moment (X3) et le quatrième moment (X4), dans lequel la période entre le premier moment (X1) et le deuxième moment (X2) est réglée en modifiant le premier moment (X1) et/ou le deuxième moment (X2), une période entre le premier moment (X1) et le troisième moment (X3) est réglée en fonction du réglage de la période entre le premier moment (X1) et le deuxième moment (X2) en modifiant le troisième moment (X3), et le troisième moment (X3) se situe après le premier moment (X1), et le quatrième moment (X4) se situe après le deuxième moment (X2), dans lequel la période entre le premier moment (X1) et le troisième moment (X3) est prolongée lorsque la période entre le premier moment (X1) et le deuxième moment (X2) est raccourcie.
  2. Procédé selon la revendication 1, dans lequel le système à colonne de rectification (10) présente une colonne haute pression (11) fonctionnant à un premier niveau de pression et une colonne basse pression (12) fonctionnant à un second niveau de pression inférieur à la première pression de fonctionnement, dans lequel un distillat de tête gazeux riche en azote est formé dans la colonne basse pression (11).
  3. Procédé selon la revendication 2, dans lequel le liquide dont la quantité est modifiée pendant la troisième période de fonctionnement (T3) est une fraction du distillat de tête gazeux riche en azote de la colonne haute pression (11) qui est liquéfié et chargé en tant que reflux dans la colonne basse pression (12).
  4. Procédé selon la revendication 2 ou la revendication 3, dans lequel le premier niveau de pression va de 5 à 12 bar de pression absolue et/ou le deuxième niveau de pression va de 1,3 à 3,5 bar de pression absolue.
  5. Procédé selon l'une des revendications 2 à 4, dans lequel le ou les produits formés à partir d'air sont formés en une quantité de produit réglable, dans lequel la quantité de produit est réglée sur une première valeur pendant la première période de fonctionnement (T1) et sur une deuxième valeur différente de la première valeur pendant la deuxième période de fonctionnement (T2), et dans lequel le réglage de la quantité de produit est modifié de la première valeur à la deuxième valeur pendant la troisième période de fonctionnement (T3) à partir du premier moment (X1) et jusqu'au deuxième moment (X2).
  6. Procédé selon la revendication 5, dans lequel le ou les produits formés à partir d'air sont formés au moins partiellement à partir du distillat de tête gazeux riche en azote de la colonne haute pression (11).
  7. Procédé selon l'une des revendications précédentes, dans lequel la première quantité d'air totale diffère de la deuxième quantité d'air totale de plus de 5 et jusqu'à 30 points de pourcentage.
  8. Procédé selon la revendication 7, dans lequel la modification de la quantité d'air totale pendant la troisième période de fonctionnement (T3) est effectuée par paliers ou en continu.
  9. Procédé selon la revendication 8, dans lequel un taux de modification moyen lors de la modification par paliers ou un taux de modification lors de la modification continue de la quantité d'air totale pendant la troisième période de fonctionnement (T3) va de 0,1 à 10 points de pourcentage par minute.
  10. Procédé selon l'une des revendications précédentes, dans lequel le système à colonne de rectification (10) présente une ou plusieurs colonnes de rectification configurées pour obtenir un produit formé à partir d'air riche en argon, et dans lequel le produit formé à partir d'air riche en argon est formé dans le procédé.
  11. Installation de séparation d'air (100) configurée pour obtenir un ou plusieurs produits formés à partir d'air et présentant un système à colonne de rectification (10), dans lequel l'installation de séparation d'air (100) est configurée pour traiter de l'air comprimé dans une quantité d'air totale réglable dans le système à colonne de rectification (100) et pour ainsi régler la quantité d'air totale sur une première valeur pendant une première période de fonctionnement (T1) et sur une deuxième valeur différente de la première valeur pendant une deuxième période de fonctionnement (T2), ainsi que de modifier le réglage de la quantité d'air totale de la première valeur à la deuxième valeur pendant une troisième période de fonctionnement (T3) à partir d'un premier moment (X1) et jusqu'à un deuxième moment (X2), dans laquelle la deuxième période de fonctionnement (T2) se situe après la première période de fonctionnement (T1) et la troisième période de fonctionnement (T3) se situe entre la première période de fonctionnement (T1) et la deuxième période de fonctionnement (T2), dans laquelle l'installation de séparation d'air (100) présente une unité de commande (50) configurée par la technique de programme pour modifier un réglage d'une quantité d'un liquide formé par rectification à l'aide de l'air comprimé et transporté dans le système à colonne de rectification (10) ou hors de celui-ci, pendant la troisième période de fonctionnement (T3), à partir d'un troisième moment (X3) et jusqu'à un quatrième moment (X4), dans laquelle le troisième moment (X3) se situe avant ou après le premier moment (X1) et avant le deuxième moment (X2) et le quatrième moment (X4) se situe après le premier moment (X1) et le troisième moment (X3) et avant ou après le deuxième moment (X2), une période entre le premier moment (X1) et le deuxième moment (X2) est réglée de telle sorte qu'elle ne diffère pas de plus de 20 % d'une période entre le troisième moment (X3) et le quatrième moment (X4), dans laquelle une période entre le premier moment (X1) et le deuxième moment (X2) est réglée en modifiant le premier moment (X1) et/ou le deuxième moment (X2), une période entre le premier moment (X1) et le troisième moment (X3) est réglée en fonction du réglage de la période entre le premier moment (X1) et le deuxième moment (X2) en modifiant le troisième moment (X3), et le troisième moment (X3) se situe après le premier moment (X1), et le quatrième moment (X4) se situe après le deuxième moment (X2), dans laquelle la période entre le premier moment (X1) et le troisième moment (X3) est prolongée lorsque la période entre le premier moment (X1) et le deuxième moment (X2) est raccourcie.
  12. Installation de séparation d'air (100) selon la revendication 11, dans laquelle le système à colonne de rectification (10) présente une colonne haute pression (11) fonctionnant à un premier niveau de pression et une colonne basse pression (12) fonctionnant à un second niveau de pression inférieur à la première pression de fonctionnement, dans laquelle l'installation de séparation d'air est réalisée pour qu'un distillat de tête gazeux riche en azote soit formé dans la colonne basse pression,
    et est en particulier réalisée pour que le liquide dont la quantité est modifiée pendant la troisième période de fonctionnement (T3) soit une fraction du distillat de tête gazeux riche en azote de la colonne haute pression qui est liquéfié et chargé en tant que reflux dans la colonne basse pression, et/ou est en particulier réalisée pour que le premier niveau de pression aille de 5 à 12 bar de pression absolue et pour que le second niveau de pression aille de 1,3 à 3,5 bar de pression absolue ;
    et/ou dans laquelle le système à colonne de rectification présente une ou plusieurs colonnes de rectification configurées pour obtenir un produit formé à partir d'air riche en argon, et l'installation de séparation d'air est réalisée pour former le produit formé à partir d'air riche en argon,
    et/ou dans laquelle l'unité de commande (50) est configurée par la technique de programme pour exécuter un procédé selon l'une des revendications 5 à 9.
EP19797562.6A 2018-10-09 2019-10-08 Procédé de production d'un ou d'une pluralité de produits gonflables et installation de séparation de l'air Active EP3864357B1 (fr)

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PCT/EP2019/025332 WO2020074120A1 (fr) 2018-10-09 2019-10-08 Procédé pour produire un ou plusieurs produits formés à partir d'air et installation de séparation d'air

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CN112654827B (zh) 2022-12-06
US12158303B2 (en) 2024-12-03
CN112654827A (zh) 2021-04-13
US20220026145A1 (en) 2022-01-27
KR20210070988A (ko) 2021-06-15
WO2020074120A1 (fr) 2020-04-16
EP3864357C0 (fr) 2025-07-23
KR102912249B1 (ko) 2026-01-15

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