EP3864357A1 - Procédé pour produire un ou plusieurs produits formés à partir d'air et installation de séparation d'air - Google Patents

Procédé pour produire un ou plusieurs produits formés à partir d'air et installation de séparation d'air

Info

Publication number
EP3864357A1
EP3864357A1 EP19797562.6A EP19797562A EP3864357A1 EP 3864357 A1 EP3864357 A1 EP 3864357A1 EP 19797562 A EP19797562 A EP 19797562A EP 3864357 A1 EP3864357 A1 EP 3864357A1
Authority
EP
European Patent Office
Prior art keywords
time
operating period
air
point
value
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
EP19797562.6A
Other languages
German (de)
English (en)
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
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 EP3864357A1 publication Critical patent/EP3864357A1/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
    • F25J3/04472—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
    • F25J3/04006—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
    • F25J3/04763—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 method for obtaining one or more air products and a corresponding air separation plant according to the respective preambles of the independent 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 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 production of nitrogen and / or oxygen in a liquid and / or gaseous state ie the rectification columns for nitrogen-oxygen separation, rectification columns for the production of further air components, in particular the noble gases krypton, xenon and / or argon, can be provided. Even if rectification columns for obtaining further air components are not specifically discussed below, 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 a pressure column, medium pressure column or lower column) and a so-called low pressure column (also referred to as an 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 approximately 1.4 bar.
  • the pressure levels given here and below are absolute pressures that at the top of each of the columns mentioned. The values mentioned are only examples that can be changed if necessary.
  • US 4,251,248 A discloses a method and apparatus for automatically changing operations in an air separation plant to increase or decrease product quantities. Intended change values, among other things for feed air, are calculated from the values of the correspondingly increased or decreased product quantities.
  • purities of air products are kept substantially constant with fluctuations in the demand for one of the products or the amount or pressure of the feed air by introducing an excess of nitrogen-rich liquid into the rectification column system when the demand for the product or the amount of feed air increases and by withdrawing and storing an excess of nitrogen-rich liquid from the distillation apparatus as the demand for the product or the amount of feed air decreases.
  • a cryogenic air separation plant which is subject to periods with considerable changes in product demand, is the subject of US 6 006 546 A.
  • the plant is specifically controlled during these periods in order to minimize the effects of transient operation on the product purity.
  • load changes Corresponding switching processes are also referred to below as "load changes". It can be assumed that rapid load changes lead to an overall higher efficiency of an air separation plant. In addition, in the event that rapid load changes are implemented, backup memories with less
  • the object of the present invention is to make the extraction of air products more flexible using air separation plants and to enable faster load changes overall.
  • This task is accomplished by a method of obtaining one or more
  • main compressors / post-compressors Main Air Compressor / Booster Air Compressor, MAC-BAC processes or so-called
  • High air pressure (HAP) processes can be used.
  • the main compressor / post-compressor process is the rather
  • the present invention is suitable for both applications.
  • the main compressor / post-compressor process is characterized in that only a part of the total amount of feed air supplied to the rectification column system is compressed to a pressure level that is significant, i.e. is at least 3, 4, 5, 6, 7, 8, 9 or 10 bar, above the pressure level of the high pressure column. Another part of the amount of air used is only the pressure level of the high pressure column or a pressure level that is not more than 1 to 2 bar from the pressure level of the
  • High-pressure column differentiates, compresses, and is fed into the high-pressure column at this lower pressure level.
  • An example of a main compressor / post-compressor process is shown by Häring (see above) in Figure 2.3A.
  • Rectification column system total amount of feed air supplied
  • Compressed pressure level that is, i.e. is at least 3, 4, 5, 6, 7, 8, 9 or 10 bar above the pressure level of the high pressure column.
  • the pressure difference can be up to 14, 16, 18 or 20 bar, for example.
  • High air pressure processes are known for example from EP 2 980 514 A1 and EP 2 963 367 A1.
  • the present invention can be used in air separation plants with so-called
  • Internal compression Internal Compression, IC
  • air separation plants with external compression.
  • at least one product which is provided by means of the air separation plant is formed by removing a cryogenic liquid from the rectification column system, subjecting it to a pressure increase in the liquid state, and, depending on the pressure present, by heating either in the gaseous or in the supercritical state is transferred.
  • internally compressed gaseous oxygen GOX IV, GOX IC
  • GAN IV, GAN IC internally compressed gaseous nitrogen
  • GAR IV GAR argon
  • Liquids and gases can be rich or poor in one or more components in the language used here, "rich” for a content of at least 90%, 95%, 99%, 99.5%, 99.9% or 99.99 % and "poor” for a content of at most 10%, 5%, 1%, 0.1% or 0.01% on mole, weight or
  • Liquids and gases can, in the language used here, be enriched or depleted in one or more components, these terms relating to a content in a starting liquid or gas from which the liquid or gas under consideration 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, and " depleted "if this or this contains at most 0.9 times, 0.5, 0.1 times, 0.01 times or 0.001 times the content of a corresponding component, based on the starting liquid or gas. If, for example, "oxygen” is used here, this also means a liquid or a gas that is rich in
  • pressures and temperatures are typically in certain ranges, for example ⁇ 1%, 5%, 10% or 20% around an average.
  • Corresponding pressure levels and temperature levels can lie in disjoint areas or in areas that overlap one another.
  • pressure levels include, for example, unavoidable or expected pressure drops.
  • the pressure levels given here in bar are absolute pressures.
  • the reason for this is the amount of cryogenic liquids stored on the dividing plates or in liquid distributors and packs of the rectification columns, in particular the high and low pressure columns. This amount of liquid depends on the load: the lower the load, the less liquid is distributed on the partitions. When the load is reduced, excess liquid is released. This excess liquid should be stored in the system so that it can be used to compensate for the deficit if the load increases.
  • Main capacitor or a so-called secondary capacitor, should be off
  • Air separation plant shows. It goes without saying that "fast" controllers are also required for fast load changes, which only lead to small deviations between setpoint and actual values.
  • Rapid load changes can lead to changed product compositions. If, for example, the air separation plant illustrated in FIG. 1 is operated with an otherwise unchanged operation at an increased load change speed (75% load to 100% load at 4% per minute), an increase in
  • Rectification column system processed amount of air is made. This can take place in the form of a delayed setpoint adjustment, in particular, as described in the following, in particular with regard to the amount of a nitrogen-rich liquid which is produced from a top product of the
  • High pressure column is formed.
  • the present invention is not limited to this specific case. Rather, the basic finding of the invention consists in the fact that a leading or trailing adjustment of corresponding fluid flows or their amounts in corresponding
  • Deployment scenarios can be particularly advantageous.
  • the present invention proposes a method for
  • total air volume is set to a first value during a first operating period and to a second value that differs from the first value during a second operating period. There are therefore different total air volumes in these two operating periods, the first total air volume being larger or smaller than the second
  • Total air volume can be.
  • a corresponding air separation plant is therefore operated in the first and the second operating period in different load conditions, in particular in one of the two operating periods
  • the present invention relates to cases of load increase and load reduction.
  • the setting of the total air quantity is changed from the first value to the second value in a third operating period from a first point in time and up to a second point in time, that is to say a load change is carried out.
  • the second operating period lies after the first operating period and the third operating period lies between the first operating period and the second operating period. Without further measures, as mentioned, this can lead to the disadvantageous effects explained.
  • a load change can represent a load increase or load reduction, depending on whether the first total air volume is less or higher than the second total air volume.
  • the first, second and third operating periods represent operating periods that do not overlap one another and the third
  • the operating period is always between the first and the second or the second and the first operating period. This does not exclude the existence of other operating periods.
  • a setting of an amount of a liquid which is formed by rectification using the compressed air and transported in or out of the rectification column system is changed from a third point in time and up to a fourth point in time, the third point in time before or after the first time and before the second time and the fourth
  • the first, the second, the third and the fourth point in time each lie within the third operating period, but for example the third may be before the first or the fourth after the second point in time, that is to say the third operating period does not have to begin with the first point in time and end at the second point in time.
  • the third operating period can lie between the earliest time and the latest time of these times, but can also extend over a longer period.
  • a period between the first point in time and the second point in time is set such 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.
  • Periods can also be set the same or essentially the same.
  • the setting can be made in particular by using appropriate setpoints or default values in a regulation or control.
  • a change in the amount of the fluid, which is generated by rectification using the compressed air and transported in or out of the rectification column system is not synchronized with the change in the total amount of air.
  • This change is made 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.
  • a corresponding control or regulation can take place in particular on the basis of recorded actual values and thereby include all measures known from the field of control or regulation technology, insofar as they are suitable and expedient for use in the present invention.
  • a corresponding controller output is additionally readjusted (typically in a range of not more than ⁇ 5%) by a trim controller. In extreme cases, this can mean that an actual value at the end of the adjustment differs slightly (but at most by 5%) from an opposite setpoint.
  • 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, the liquid, the amount of which is changed in the third operating period, as mentioned Part of a gaseous nitrogen-rich top product of the high pressure column, which is liquefied and fed as a return 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.
  • a secondary condenser for heating an internally compressed oxygen product.
  • internal or external compression of air products can and can
  • Air separation plants with several high pressure columns can also be used.
  • the first pressure level in the context of the present invention can in particular be 5 or 7 to 12 bar
  • Absolute pressure and the second pressure level are in particular 1, 3 or 1, 8 to 3.5 bar absolute pressure.
  • the present invention can thus be used in particular in so-called “elevated pressure” air separation plants in which the operating pressures of the distillation column systems are above the conventional values mentioned at the outset. Nevertheless, the invention can also be used in connection with conventional pressure levels in the distillation column system.
  • Period between the first point in time and the second point in time can be set by changing the first point in time and / or the second point in time.
  • a delay time provided within the scope of the present invention is applied to it
  • Change is adjusted, i.e. if a period between the first point in time and the third point in time depends on the setting of the period between the first point in time and the second point in time by changing the third
  • Time is set. In this way you can also change Load change speeds achieve the advantages of the invention.
  • a longer delay time can be selected.
  • a change in load can in particular also include changing the quantities of the air products formed in each case.
  • One or more air products can therefore be formed in an adjustable product quantity, the product quantity being set to a first value during the first operating period and to a second value different from the first value during the second operating period, and wherein the setting the amount of product is changed in the third operating period from the first point in time and up to the second point in time from the first value to the second value.
  • a corresponding air product can in particular be such an air product that is at least partially formed from the gaseous nitrogen-rich top product of the high-pressure column. This can be provided in liquefied or non-liquefied form.
  • the present invention can be related to various aspects
  • Load change scopes are used.
  • the first total air volume differs from the second total air volume by more than 5 and up to 30, 40 or 50 percentage points.
  • the change in the total air volume can take place gradually or continuously in the third operating period, and preferably with an average rate of change (based on the gradual change) or a rate of change (in the case of continuous change) of the total air volume of 0.1 (in the case of extraction) of argon) or 1 to 10 percentage points per minute.
  • argon extraction can be provided in the context of the present invention, ie in the method the rectification column system can in particular one or more for the extraction of an argon-rich air product have rectification columns set up and the argon-rich air product can be formed in the process.
  • An "argon-rich" air product has at least 50, 60, 70, 80 or 90 mole percent argon.
  • the present invention also extends to an air separation plant which is set up to obtain one or more air products and a
  • Rectification column system wherein the air separation plant is set up to supply compressed air in an adjustable total amount of air
  • the second operating period lies after the first operating period and 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, which is set up for programming purposes in the third operating period
  • the control unit is set up, in particular, in terms of program technology
  • FIG. 1 shows an air separation plant that can be operated in accordance with an embodiment of the invention in the form of a simplified process flow diagram.
  • Figure 2 shows changes in material flows and their compositions in a method not according to the invention in the form of a diagram.
  • Figure 3 shows changes in material flows and their compositions in a method according to an embodiment of the invention in the form of a diagram.
  • Figure 4 shows changes in material flows and their compositions in a method according to an embodiment of the invention in the form of a diagram.
  • FIG. 1 an air separation plant that can be operated in accordance with 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, the one
  • High pressure column 11 and a low pressure column 12 includes.
  • feed air (A) is drawn in and compressed by means of a main air compressor 1 via a filter 2.
  • Compressed air stream a is precooled and cleaned in a generally known manner in a pre-cooling device 3 operated with cooling water (B) and a cleaning device 4. Air of the pre-cooled and cleaned compressed air stream a is fed to a main heat exchanger 5 on the warm side in the form of two partial streams b and c.
  • the partial flow b is the main heat exchanger 5 on one
  • the intermediate temperature level is removed and expanded (blown) into the low-pressure column 12 by means of a blowing-in turbine 6, which can be coupled to an oil brake or a generator that is not specifically designated.
  • the partial flow c is taken from the main heat exchanger 5 on the cold side, by a blowing-in turbine 6, which can be coupled to an oil brake or a generator that is not specifically designated.
  • the partial flow c is taken from the main heat exchanger 5 on the cold side, by a
  • Auxiliary condenser 7 out and fed into the high pressure column 1 1 via a valve not specifically designated.
  • 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 in the form of a stream d through a countercooling countercurrent 8 and into the
  • Low pressure column 12 fed.
  • the top product of the high-pressure column 11 is liquefied partly in the form of a stream e in a main condenser 13 which connects the high-pressure column 11 and the low-pressure column 12 in a heat-exchanging manner, and partly in the form of a stream f in the main heat exchanger 5 and is heated as a gaseous one
  • the liquefied fraction is partly returned in the form of a stream g to the high-pressure column 11 as a return line, and in particular in further adjustable proportions it is fed in the form of a stream h into a tank 20 and in the form of a stream i through the supercooling counterflow 8 and onto it Low pressure column 12 abandoned.
  • An oxygen-rich liquid sump product is formed in the low-pressure column 12 and pressure-increased in the form of a material flow k in an internal compression pump 9 in the liquid state. At least a part 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 in the form of a material flow m can be fed back into the low-pressure column 12 via a valve, which is not specifically designated. In the secondary condenser 7, the material flow I is evaporated, at least for the most part. A correspondingly evaporated stream n is in
  • Main heat exchanger 5 is heated, in the process converted from the liquid to the gaseous or supercritical state and designed as a gaseous pressurized oxygen product (C) from the air separation plant 100.
  • a fill level in a liquid container of the secondary condenser 7 is regulated by the inlet flow I. If necessary, liquid can be released into the atmosphere (D) in the form of a stream o.
  • a liquid level in the liquid container of the secondary condenser 7, but also a liquid level in the low pressure column 12 and thus in a liquid container of the main condenser 13 should, as mentioned, be kept constant for safety reasons. This essentially leaves the sump of the high-pressure column 11 in the air separation plant 100 illustrated here as a possible one
  • Air separation plant head gas is drawn off in the form of a material flow p and partly in the form of a material flow q through the supercooling counterflow 8 and the
  • Low pressure column 12 is withdrawn.
  • the last-mentioned material flows can be used in various ways in the air separation plant 100, provided as a product, and / or released into the atmosphere (D).
  • the tank 20 can in particular be used to buffer a return flow to the low pressure column 12.
  • the i can be provided in the form of the material flow
  • nitrogen-rich liquid for the operation of the low-pressure column 12 is not sufficient, a corresponding addition can be made by means of a stream of material s from the tank 20, and if the amount of such a nitrogen-rich
  • Liquid exceeds the demand for product or the need in the air separation plant 100, a feed into the tank 20 can be made.
  • Figure 2 shows changes in material flows and their compositions in a method not according to the invention in the form of a diagram, with a time in Minutes is plotted on the abscissa compared to a normalized range of values from 0 to 100% on the ordinate.
  • the representation of FIG. 1 corresponds to that of FIGS. 3 and 4, with the latter in each case corresponding changes in
  • Air quantity 101 is set to a first value and, during a second operating period T2, to a second value that differs from the first value.
  • the corresponding guide vane position of the main air compressor is designated 101 ', the specification (ramp) for the guide vane position is designated 101 ".
  • the same also applies to the amount of a gaseous nitrogen-rich top product of a high-pressure column of a corresponding system, which liquefies and returns to the
  • Oxygen content 103 in a top product of the high pressure column is temporarily greatly increased here. This goes with a temporary increase in column temperature 104 of the high pressure column and with a decrease in column temperature 105 of
  • a quantity of an oxygen product removed from the air separation plant is designated by 106.
  • a third operating period T3 is therefore provided here.
  • This is, as is basically the case previously, in the
  • Distilled column system fed and processed there air quantity 101 changed from a first time X1 and up to a second time X2 from the first value to the second value.
  • the third time X3 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 FIG. 4 corresponds to the representation according to FIG. 3 over an extended period of time.
  • "purge" oxygen 107 is periodically blown off to the atmosphere (see stream o in FIG. 1) by one
  • this can also be injected into the pressurized oxygen product (C).

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)

Abstract

L'invention concerne un procédé pour produire un ou plusieurs produits formés à partir d'air, procédé au cours duquel une installation de séparation d'air (100) équipée d'un système de colonne de rectification (10) est utilisée, une quantité totale d'air sous pression ajustable y étant traitée. Cette quantité d'air totale est ajustée pour être égale à une première valeur pendant une première période de fonctionnement (T1) et pour être égale à une deuxième valeur différente de la première valeur pendant une deuxième période de fonctionnement (T2), cet ajustement de la quantité d'air totale étant modifié pendant une troisième période de fonctionnement (T3), à partir d'un premier moment (X1) jusqu'à un deuxième moment (X2), pour passer de la première à la deuxième valeur. La deuxième période de fonctionnement (T2) intervient après la première période de fonctionnement (T1), la troisième période de fonctionnement (T3) se situe entre la première période de fonctionnement (T1) et la deuxième période de fonctionnement (T2). Selon l'invention, pendant la troisième période de fonctionnement (T3), une quantité d'un liquide formé par rectification au moyen d'air sous pression est ajustée et transportée dans le système de colonne de rectification (10) ou hors de celui-ci, à partir d'un troisième moment (X3) et jusqu'à un quatrième moment (X4), le troisième moment (X3) se situant avant ou après le premier moment (X1) et avant le deuxième moment (X2), et le quatrième moment (X4) se situant après le premier moment (X1) et le troisième moment (X3) et avant ou après le deuxième moment (X2). Un intervalle de temps entre le premier moment (X1) et le deuxième moment (X2) est ajusté de manière à être sensiblement égal à un intervalle de temps entre le troisième moment (X3) et le quatrième moment (X4). Cette invention concerne en outre une installation de séparation d'air (100) correspondante.
EP19797562.6A 2018-10-09 2019-10-08 Procédé pour produire un ou plusieurs produits formés à partir d'air et installation de séparation d'air Pending EP3864357A1 (fr)

Applications Claiming Priority (2)

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EP18020489 2018-10-09
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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US (1) US20220026145A1 (fr)
EP (1) EP3864357A1 (fr)
KR (1) KR20210070988A (fr)
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WO (1) WO2020074120A1 (fr)

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DE202021002895U1 (de) * 2021-09-07 2022-02-09 Linde GmbH Anlage zur Tieftemperaturzerlegung von Luft

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US20220026145A1 (en) 2022-01-27
CN112654827A (zh) 2021-04-13
KR20210070988A (ko) 2021-06-15
WO2020074120A1 (fr) 2020-04-16

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