WO2019201475A1 - Procédé pour faire fonctionner un échangeur de chaleur, ensemble pourvu d'un échangeur de chaleur et installation de traitement d'air pourvue d'un ensemble correspondant - Google Patents

Procédé pour faire fonctionner un échangeur de chaleur, ensemble pourvu d'un échangeur de chaleur et installation de traitement d'air pourvue d'un ensemble correspondant Download PDF

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Publication number
WO2019201475A1
WO2019201475A1 PCT/EP2019/025097 EP2019025097W WO2019201475A1 WO 2019201475 A1 WO2019201475 A1 WO 2019201475A1 EP 2019025097 W EP2019025097 W EP 2019025097W WO 2019201475 A1 WO2019201475 A1 WO 2019201475A1
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Prior art keywords
exchange zone
zone
temperature level
operating mode
exchange
Prior art date
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PCT/EP2019/025097
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German (de)
English (en)
Inventor
Lars Kirchner
Original Assignee
Linde Aktiengesellschaft
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Publication of WO2019201475A1 publication Critical patent/WO2019201475A1/fr

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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
    • F25J3/04406—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system
    • F25J3/04412—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air using a dual pressure main column system in a classical double column flowsheet, i.e. with thermal coupling by a main reboiler-condenser in the bottom of low pressure respectively top of high pressure column
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/04084—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of nitrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04006—Providing pressurised feed air or process streams within or from the air fractionation unit
    • F25J3/04078—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression
    • F25J3/0409—Providing pressurised feed air or process streams within or from the air fractionation unit providing pressurized products by liquid compression and vaporisation with cold recovery, i.e. so-called internal compression of oxygen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04151—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
    • 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
    • F25J3/04763—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
    • F25J3/04787—Heat exchange, e.g. main heat exchange line; Subcooler, external reboiler-condenser
    • 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
    • F25J3/04824—Stopping of the process, e.g. defrosting or deriming; Back-up procedures
    • 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
    • F25J5/00—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants
    • F25J5/002—Arrangements of cold exchangers or cold accumulators in separation or liquefaction plants for continuously recuperating cold, i.e. in a so-called recuperative heat exchanger
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
    • F25J2290/32—Details on header or distribution passages of heat exchangers, e.g. of reboiler-condenser or plate heat exchangers
    • 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
    • F25J2290/44—Particular materials used, e.g. copper, steel or alloys thereof or surface treatments used, e.g. enhanced surface

Definitions

  • the invention relates to a method for operating a heat exchanger and an arrangement with a corresponding operable heat exchanger according to the
  • heat exchangers with cryogenic fluids i. Fluids with temperatures of well below 0 ° C, especially well below -100 ° C, operated.
  • the present invention will be described mainly with reference to the main heat exchangers of air separation plants, but it is also suitable, for example, for systems for storing and recovering energy using liquid air.
  • the main heat exchangers of air separation plants are characterized in particular by the fact that in them at least a part of the air to be processed is cooled from ambient temperature or above to a temperature close to the liquefaction temperature.
  • the temperature profiles at standstill of the associated system are the same for corresponding heat exchangers. Will then, for example, when restarting in a heated part of the
  • Heat exchanger feeds cryogenic gas or vice versa warm gas in a cooled part of the heat exchanger, it comes to high thermal stresses, which can lead to damage to the heat exchanger or require a disproportionately high material or manufacturing costs.
  • Heat exchanger warmer until the temperatures mentioned are at or near an average temperature This is also illustrated again in the appended FIG.
  • a method for preventing cold losses in an air separation plant is known from KR 2003-0056252 A.
  • the air separation plant is doing with additional Air from an adjacent air separation plant is applied when it is briefly shut down, for example for repair.
  • a method for liquefying helium is known from DE 10 201 1 003 391 A1. This includes several consecutive purification and
  • Liquefaction stages including a condensation cleaning.
  • a series of heat exchangers is used.
  • the present invention has as its object to provide measures that enable a re-commissioning of a heat exchanger used for processing of air heat exchanger after prolonged shutdown without the mentioned adverse effects.
  • the present invention proposes a method for operating a heat exchanger and an arrangement with a corresponding operable heat exchanger, which is designed as an air handling system, with the
  • a “heat exchanger” in the language used here is an apparatus that is designed for the indirect transfer of heat between at least two, for example, in countercurrent to each other guided fluid streams.
  • a heat exchanger for use in the context of the present invention may be formed from a single or a plurality of heat exchanger sections connected in parallel and / or in series, for example from one or more plate heat exchanger blocks.
  • a heat exchanger has "passages" which are set up for fluid guidance and are fluidically separated from other passages or are connected on the input and output side only via the respective headers. These are hereinafter referred to as "heat exchanger passages". In the following, the terms “heat exchanger” and “heat exchanger” are used synonymously.
  • the present invention relates to the apparatuses referred to as rib-plate heat exchangers according to the German version of ISO 15547-2: 2005 (Plate-Fin Heat Exchangers). Is below a "heat exchanger" the speech, therefore, this is understood in particular a ribbed plate heat exchanger.
  • a fin-plate heat exchanger has a plurality
  • soldered plates i.d.R. made of aluminum
  • the plates are stabilized by side bars and connected with each other via side bars.
  • the structuring of the heat exchanger plates serves in particular to increase the heat exchange surface, but also to increase the stability of the heat exchanger. More particularly, the invention relates to brazed aluminum ribbed plate heat exchangers.
  • the present invention can be used in air separation plants of known type, but also for example in plants for storing and recovering energy using liquid air.
  • LAES Liquid Air Energy Storage
  • LAES plants in a first mode of operation compress air, cool it, liquefy it and store it in an isolated tank system.
  • low supply of electricity in a second mode of operation stored in the tank system liquefied air, in particular after an increase in pressure by means of a pump, warmed and thus converted into the gaseous or supercritical state.
  • a pressurized stream obtained thereby is expanded in an expansion turbine which is coupled to a generator. The electrical energy gained in the generator is
  • a corresponding storage and recovery of energy is basically not only possible using liquid air. Rather, in the first mode of operation, other deep-free formed using air may also be used
  • Liquids stored and in the second mode of operation for obtaining electrical energy can be used.
  • Liquids are liquid nitrogen or liquid oxygen or
  • Component mixtures consisting predominantly of liquid nitrogen or liquid oxygen.
  • external heat and fuel can also be coupled in order to increase the efficiency and the output, in particular by using a gas turbine whose exhaust gas is expanded together with the pressure stream formed from the air product in the second operating mode.
  • the invention is suitable.
  • Air separation plants serve. If liquid air is used, it is also possible to use pure air liquefaction plants. As a generic term for
  • Air separation plants and air liquefaction plants the term “air handling equipment” is therefore used below.
  • air separation plant By means of an air separation plant and by means of an air liquefaction plant can be used here
  • air products are provided, wherein an air product of an air separation plant is a cryogenically produced air fraction and an air product of an air liquefaction plant is (also cryogenically produced) liquid air.
  • An air fraction has one or more components of atmospheric air in a different content than in the atmospheric air or consists exclusively of these or these components.
  • a cryogenic production involves cooling to a temperature level of less than -100 ° C. Even an air separation plant liquid air can be removed as an air product.
  • a heat exchanger can be flowed through during a standstill of the associated system with cold gas from a tank or exhaust gas from the stationary system in order to avoid heating or to keep the formed temperature profile.
  • cold gas from a tank or exhaust gas from the stationary system in order to avoid heating or to keep the formed temperature profile.
  • exhaust gas from the stationary system in order to avoid heating or to keep the formed temperature profile.
  • the present invention proposes a method of operating a heat exchanger having a first exchange zone having a first end and a second end, a second exchange zone having a first end and a second end, and a separation zone between the first end of the first exchange zone and the first exchange zone second end of the second exchange zone, wherein a heat conductivity of the first exchange zone between the first end and the second end and a heat conductivity of the second exchange zone between the first end and the second end each higher than a thermal conductivity of the separation zone between the second end of the first exchange zone and the first end of the second exchange zone.
  • the heat exchanger can, as also explained in detail below, be the main heat exchanger of an air separation plant, so that reference may be made in this connection to the cited technical literature.
  • a corresponding heat exchanger is a fin-plate heat exchanger of the type described above.
  • the "exchange zones" are those zones of a corresponding heat exchanger in which fluid streams are subjected to mutual heat exchange.
  • the heat exchanger used in the context of the present invention may for example be designed as a heat exchanger, which is constructed from two parts or two separate serial individual heat exchangers. Corresponding parts or Individual heat exchangers each define areas of separate heat exchange, ie the "exchange areas" of the type explained above.
  • Decommissioning also a temperature compensation between the respective hot and cold end. Due to the fact that the temperature profile in each of the parts or individual heat exchanger of a trained accordingly
  • Heat exchanger does not extend from the highest to the lowest temperature level of the total heat exchanger, but only up to or from one
  • Single heat exchangers is present, can initially by a heat conduction within the respective part or individual heat exchanger only a middle
  • Temperature level can be reached, the between the temperature level at the warm end and the intermediate temperature level on the one hand or between the
  • This mean temperature level is higher in a part or single heat exchanger at the warm end and lower in a part or individual heat exchanger at the cold end than the average temperature level in a one-piece
  • Heat exchanger This results from the fact that in a multi-part heat exchanger, a heat conduction between the respective parts can be prevented or reduced.
  • a temperature level of, for example, about -50.degree. C. and, for example, about -150.degree. C. in the cold part results in a warm part of a corresponding two-part heat exchanger.
  • This also halves the maximum possible temperature differences between metal and the warm or cold streams fed into the heat exchanger when restarted, which means that the thermal stresses are only fractions in comparison to the usual heat exchanger configuration.
  • the present invention provides that in a first mode of operation by passing fluids through the first exchange zone and through the second
  • Temperature level is controlled and tempered the second end of the second exchange zone to a second temperature level below the first temperature level becomes.
  • the first operating mode corresponds to the regular operation of a corresponding heat exchanger, for example in an air separation plant. In this regular operation, warm fluids are fed into the warm end of the heat exchanger and cold fluids are fed to the cold end and directed towards each other.
  • the first temperature level can in the context of the present invention, in particular at 0 to 100 ° C, for example, about 20 ° C, and the second
  • Temperature level at -100 to -200 ° C, for example, about -175 ° C are.
  • the passage of fluid takes place, in particular, in the form of a plurality of different fluid streams, which are directed towards one another and thus directed in opposite directions through the first and the second exchange zones.
  • a temperature level is established which lies between the first and the second temperature level.
  • the present invention relates to the cryogenic processing of air in the form of a cryogenic separation of air or a pure one
  • Air liquefaction such that the fluids passed through the first exchange zone and the second exchange zone in the first mode of operation comprise pressurized dried air and, in particular countercurrently thereto, at least one cryogenic air product formed using the pressurized dried air.
  • Adsorption may be part of the proposed method according to the invention, as well as the formation of at least one cryogenically formed air product.
  • the first operating mode is interrupted by a second operating mode, in which the passage of the fluids, that is the pressurized dried air and the cryogenically formed or
  • An inhibition of the passage exists in particular in a complete setting of the passage, However, it can also be provided to prevent the passage only partially, as also explained below. As already explained above, this results in a slow temperature adjustment between the first end and the second end of the first exchange zone and the first end and the second end of the second exchange zone. A total temperature adjustment is likewise to be observed here. However, this is done in the context of the present invention, in which a heat exchanger with two exchange zones and a separation zone with lower heat conduction is used, much slower than in a heat exchanger having only one exchange zone, for example, only a single heat exchanger block.
  • a higher compensation temperature level arises in the first exchange zone and a lower compensation temperature level in the second exchange zone.
  • the two exchange zones are present at sufficiently different temperature levels, in other words the temperature of the first exchange zone is sufficiently high and the temperature of the second
  • the first exchange zone can be acted upon with a warm fluid at the first temperature level and the second exchange zone with a cold fluid at the second temperature level, without it being possible here for excessively high thermal stresses in each case one
  • the second operating mode is interrupted and the first operating mode or another operating mode is initiated as soon as a variable between one of the first end and the second end of the first exchange zone and / or between the first end and the second end characterized the second exchange zone heat transfer after the initiation of the second mode of operation, exceeds or falls below a predetermined value.
  • Temperature level and / or a measured or expected in the second exchange zone temperature level can be used. If, for example, a measured temperature value drops below a certain value at the first end of the first exchange zone, this indicates that heat transfer has taken place between the first exchange zone first and second ends of the first exchange zone to a certain extent. On the other hand, for example, rises at the second end of the second
  • Temperature average values may also be used based on measured values, for example an average between a measured temperature at the first and second ends of the first exchange zone and an average value between a measured temperature at the first and second ends of the second
  • expected temperature values can also be used in a corresponding manner. For example, due to
  • Temperature measurement can be defined on a test heat exchanger in the laboratory, with correspondingly determined values can be transferred to identical heat exchanger in the field or extrapolated to similar type heat exchangers.
  • the size that characterizes the heat transfer that has taken place can be, in particular, a process that sets itself up in the second operating mode
  • Temperature level at the first end of the first and / or a setting in the second operating mode temperature level at the second end of the second exchange zone act. These temperature levels can be determined in particular by means of a measurement in the form of one or more temperature values.
  • Operation mode are interrupted when the temperature level at the cold end of the heat exchanger as a whole, so for example at the second end of the second exchange zone, or a corresponding other temperature value or average, has risen above a certain temperature value, but has not reached an overlying temperature value.
  • the second operating mode is interrupted when the temperature level at the warm end of the heat exchanger as a whole, ie
  • Operating mode can be safely initiated and avoiding excessive thermal stresses.
  • the present invention may also include taking into account a size which is one between the first
  • a measured or expected temperature difference between temperature levels in the first and second exchange zones may be taken into account, in particular between a mean temperature level in the first and second exchange zones or between a temperature level at the second end of the first and the first End of the second exchange zone. If such a temperature difference falls below a predetermined difference value, the second operating mode can be interrupted and the first or the further operating mode can be initiated. Instead of a
  • Temperature difference can be used in each case corresponding absolute values, taking into account whether a corresponding temperature level in the first exchange zone does not fall below a predetermined value and a corresponding temperature level in the second exchange zone does not exceed a predetermined value.
  • thermo properties of the heat exchanger or the first and the second exchange zone and the separation zone can be assumed after the lapse of a certain time at previously known conditions that a certain heat transfer has occurred. It is also at a corresponding time or at the associated expected temperature level also by a size, which took place between the first end and the second end of the first exchange zone and / or between the first end and the second end of the second exchange zone Heat transfer after the initiation of the second mode of operation features.
  • An appropriate timing may, for example, based on determined
  • the second operating mode is interrupted and the first operating mode or another operating mode is initiated, as soon as the size between the first end and the second end of the first
  • threshold values or time specifications are selected such that it is ensured that, if necessary, in each case a temperature within the first and the second heat exchange zone compensates, a temperature compensation in the heat exchanger has not taken place in total.
  • the balancing temperatures within the first and second heat exchange zone are, as mentioned, in each case closer to the first or second temperature level than a balancing temperature in the heat exchanger as a whole or in a classic one-piece heat exchanger in which a mean temperature between the first and sets the second temperature level as a compensation temperature. In this way, an interruption time can be extended within the scope of the present invention without the initiation of further temperature control measures.
  • no additional fluids need to be used, which is the
  • the second operating mode can be interrupted and, instead of resuming the first operating mode, another operating mode can be initiated as soon as the size between the first end and the second end of the first exchange zone and / or between the first End and the second end of the second exchange zone were made
  • Heat transfer after the initiation of the second mode indicates the predetermined value is above or below.
  • Operating mode may in particular also be a tempering mode in which the heat exchanger is tempered by measures known per se.
  • a flow through a corresponding heat exchanger with fluid streams can be carried out in a smaller amount per unit of time than in the first Operating mode used fluid streams can be used. In this case, the passage of appropriate fluids is thus only partially prevented or
  • the fluids passed in the first mode of operation are replaced by others.
  • the method proposed according to the invention can be carried out in particular on the basis of one or more temperatures, in particular one or more measured temperatures.
  • the size the heat transfer between the first end and the second end of the first exchange zone and / or between the first end and the second end of the second exchange zone after the initiation of the second mode of operation
  • one or more first fluids at the first temperature level of the first exchange zone are or are supplied via the first end thereof, successively through the first exchange zone, the separation zone and the second
  • a longitudinal heat conduction in a corresponding heat exchanger is reduced by the division into the first exchange zone and the second exchange zone with the intermediate separation zone.
  • This may be effected, in particular, by the choice and specific configuration of the separation zone, which in particular reduces or prevents outflow of heat from the second end of the first exchange zone to the first end of the second exchange zone.
  • Corresponding embodiments will be explained below, these explanations for a heat exchanger according to the invention and a corresponding arrangement as well as for a method according to the invention and respective embodiments thereof being valid in the same way.
  • the first exchange zone and the second exchange zone may include one or more first materials with one or more first materials have a plurality of first heat conductivity values or, in particular exclusively, be formed from one or more corresponding materials.
  • the separation zone can have one or more second materials with one or more second heat conductivities or, in particular, can be formed from one or more corresponding materials.
  • the second heat conductivity value (s) is less than the first thermal conductivity value (s).
  • Exchange zones may be aluminum in particular.
  • Separation zone may be a metal with less heat conduction or even one or more plastics.
  • first exchange zone and the second exchange zone can each have structured metal plates lying one above the other, and the separation zone can be formed without structured metal plates lying one above the other.
  • the first exchange zone and the second exchange zone can be designed in particular in the form of separate rib-plate heat exchangers, which are separated from one another by an air gap or air space or in another way and connected to one another by means of pipes.
  • the separation zone can be formed in the form of an insulating space between the first exchange zone and the second exchange zone, wherein pipes are led through the insulating space, which connect the first exchange zone and the second exchange zone.
  • Exchange zone can be formed in any form. They are thus not limited to a design as a rib-plate heat exchanger.
  • the insulating space and thus the separation zone can thus be at least partially formed as an air space or evacuated space in the context of the present invention. It is also possible that the insulating space and thus the separation zone at least partially with a
  • Insulation material is filled, in particular with an insulation material usually used in a coldbox such as perlite and the like.
  • first exchange zone and the second exchange zone lie one above the other
  • the metal plates can also be continuous metal plates with the respective different structurings.
  • the deviating structuring in the separation zone may in particular lead to the deviating heat conduction in the separation zone, for example by a material cross-section between the second end of the first exchange zone and the first end of the second exchange zone being reduced.
  • the present invention further extends to an arrangement with a
  • a heat exchanger comprising a first exchange zone having a first end and a second end, a second exchange zone having a first end and a second end and a separation zone between the first end of the first
  • Temperature levels to temper Furthermore, technical means are provided, which are set up to interrupt the first operating mode by a second operating mode, in which the passage of the fluids through the first exchange zone and the second exchange zone is prevented.
  • the arrangement according to the invention is characterized by technical means which are set up as the fluids which are conducted in the first operating mode through the first exchange zone and through the second exchange zone,
  • such a system has a control device which is designed, if necessary, for example, according to a fixed switching pattern, based on a sensor signal or on
  • the present invention also extends to a
  • Air treatment plant having means for liquefying and / or cryogenic separation of air. This is inventively characterized in that it comprises an arrangement as just explained.
  • Air processing plant be designed as an air separation plant.
  • it comprises a distillation column system of basically known type.
  • a corresponding air processing plant can in particular also be designed as a system for storing and recovering energy.
  • FIG. 1 illustrates temperature profiles in a heat exchanger according to FIG.
  • FIG. 2 illustrates an air separation plant having a heat exchanger that may be operated using a method according to an embodiment of the present invention.
  • FIG. 1 illustrates temperature profiles in a heat exchanger according to FIG.
  • Embodiments of the present invention in the form of a temperature diagram.
  • Temperature in a regular operation of the heat exchanger about 20 ° C and the temperature C at the second (cold) end about -175 ° C. These temperatures are increasingly converging over time. This is due to the high thermal conductivity of the materials installed in the heat exchanger. In other words, heat flows from the first (warm) end towards the second (cold) end.
  • Tensions come when the first (warm) end of the heat exchanger after some time of regeneration without further action again with a warm fluid of about 20 ° C is applied in the example shown.
  • FIG. 2 illustrates an air separation plant as an example of an arrangement 100 according to one embodiment of the present invention. This has as essential components a heat exchanger 10, the main heat exchanger of the
  • Air separation plant and a distillation column system 20 on.
  • Air separation plants of the type shown are, as mentioned, often described elsewhere, for example in H.-W. Haring (ed.), Industrial Gases Processing, Wiley-VCH, 2006, especially Section 2.2.5, "Cryogenic Rectification".
  • An air separation plant for use of the present invention can be designed in many different ways. The use of the present invention is not limited to the embodiment according to FIG. Figure 2 illustrates only those for the description of the present invention
  • the heat exchanger 10 comprises a here designated 1 first exchange zone with a first end 1 1 and with a second end 12 and one here with the second
  • second exchange zone having a first end 21 and a second end 22.
  • a here designated 3 separating zone is formed between the first end 1 1 of the first exchange zone 1 and the second end 12 of the second exchange zone 2.
  • the separation zone 3 is here in the form of an air space or otherwise formed, for example by means of insulation material filled space between the first exchange zone 1 and the second exchange zone 2 is formed.
  • a thermal conductivity of the first exchange zone 2 between the first end 1 1 and the second end 12 and a thermal conductivity of the second exchange zone 2 between the first end 1 1 and the second end 12 is in each case higher than a thermal conductivity of the separation zone 13 between the second end 1 the first exchange zone 1 and the first end of the second exchange zone 2.
  • a first operating mode for example in accordance with a control unit 50 shown in a very simplified manner, as described below, by passing fluids through the first exchange zone 1 and the second exchange zone 2, the first end 1 1 of the first exchange zone 1 to a first Temperature level and the second end 12 of the second exchange zone 2 tempered to a second temperature level below the first temperature level.
  • At least one compressed, purified feed air stream 101 is supplied in the first operating mode of the first exchange zone 1 via the first end 1 1, successively passed through the first exchange zone 1, the separation zone 3 and the second exchange zone 2, and then at the second temperature level of the second exchange zone 2 executed via the second end 22.
  • a partial stream 102 or a separate feed air stream can also be expanded via a decompression device 30, for example a generator turbine. The partial flow 102 is not passed through the second exchange zone here.
  • the feed air stream 101 or a residual stream 103 remaining after separation of the partial stream 102 is fed into a high-pressure column 21 of the distillation column system 20 after cooling in the heat exchanger 10 in the illustrated example.
  • the partial flow 102 is in the example shown after its relaxation in the
  • Distillation column system 20 fed.
  • Low pressure column 22 are in a known manner with each other over a
  • oxygen-enriched fluid is withdrawn in the form of a stream of material 104, passed through a supercooling countercurrent 34 and fed into the low-pressure column 22. From a lower area of the
  • Low-pressure column 22 is an oxygen-rich fluid in the form of a stream 105 and from the top of the low-pressure column, a nitrogen-rich fluid in the form of a
  • Material stream 106 deducted.
  • the stream 106 is through the
  • the streams 105 and 106 are successively supplied at the second temperature level of the second exchange zone 2 of the heat exchanger 10 via the second end 22, through the second exchange zone 2, the separation zone 3 and the first
  • the first operating mode is interrupted by a second operating mode in which the passage of fluid through the first exchange zone 1 and the second exchange zone 2 in the form of the material streams 102, 103, 105, 106 is prevented.
  • the second mode of operation is interrupted and the first mode of operation or another mode of operation is initiated as soon as a quantity equal to one between the first end 11 and the second end 12 of the first exchange zone 1 and / or between the first end 21 and the second end 22 characterized the second exchange zone 2 carried heat transfer after the initiation of the second mode of operation, as explained several times exceeds or falls below a predetermined value.
  • one or more temperature sensors 40 can be used to determine a corresponding value.

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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 faire fonctionner un échangeur de chaleur (10), qui présente une première zone d'échange (1) pourvue d'une première extrémité (11) et d'une deuxième extrémité (12), une deuxième zone d'échange (2) pourvue d'une première extrémité (21) et d'une deuxième extrémité (22) et une zone de séparation (3) entre la première extrémité (11) de la première zone d'échange (1) et la deuxième extrémité (12) de la deuxième zone d'échange (2). Les conductibilités thermiques de la première zone d'échange (2) entre la première extrémité (11) de celle-ci et la deuxième extrémité (12) de celle-ci et de la deuxième zone d'échange (2) entre la première extrémité (11) de celle-ci et la deuxième extrémité (12) de celle-ci sont respectivement plus élevées qu'une conductibilité thermique de la zone de séparation (13) entre la deuxième extrémité (11) de la première zone d'échange (1) et la première extrémité de la deuxième zone d'échange (2). Dans un premier mode de fonctionnement, un passage de fluides à travers la première zone d'échange (1) et à travers la deuxième zone d'échange (2) permet de thermo-réguler la première extrémité (11) de la première zone d'échange (1) à un premier niveau de température et la deuxième extrémité (12) de la deuxième zone d'échange (2) à un deuxième niveau de température au-dessous du premier niveau de température. Le premier mode de fonctionnement est interrompu par un deuxième mode de fonctionnement, dans lequel le passage des fluides à travers la première zone d'échange (1) et la deuxième zone d'échange (2) est empêché. Selon l'invention, les fluides, qui sont guidés dans le premier mode de fonctionnement à travers la première zone d'échange (1) et à travers la deuxième zone d'échange (2), comprennent de l'air séché sollicité en pression et au moins un produit d'air formé de manière cryogénique au moyen de l'air séché sollicité en pression, et le deuxième mode de fonctionnement est interrompu et le premier mode de fonctionnement ou un autre mode de fonctionnement est activé dès qu'une grandeur, qui caractérise un transport de chaleur effectué entre la première extrémité (11) et la deuxième extrémité (12) de la première zone d'échange (1) et/ou entre la première extrémité (21) et la deuxième extrémité (22) de la deuxième zone d'échange (2) après l'activation du deuxième mode de fonctionnement, dépasse une valeur prédéfinie ou passe au-dessous de celle-ci. L'invention concerne également un ensemble correspondant.
PCT/EP2019/025097 2018-04-19 2019-04-03 Procédé pour faire fonctionner un échangeur de chaleur, ensemble pourvu d'un échangeur de chaleur et installation de traitement d'air pourvue d'un ensemble correspondant WO2019201475A1 (fr)

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EP18020163.4A EP3557165A1 (fr) 2018-04-19 2018-04-19 Procédé de fonctionnement d'un échangeur thermique, système doté d'un échangeur thermique et installation d'alimentation en air dotée d'un tel système

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US20210140710A1 (en) * 2019-11-07 2021-05-13 Conocophillips Company Systems and methods for removing nitrogen during liquefaction of natural gas

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US5233839A (en) 1991-03-13 1993-08-10 L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Process for operating a heat exchanger
KR20030046252A (ko) * 2001-12-05 2003-06-12 주식회사 포스코 공기분리장치의 한냉손실방지를 위한 운전방법
KR20030056252A (ko) 2001-12-27 2003-07-04 엘지.필립스 엘시디 주식회사 폴리실리콘 박막 제조방법
DE102011003391A1 (de) 2011-01-31 2012-08-02 Linde Aktiengesellschaft Anlage zum kryotechnischen Verflüssigen eines Gases oder Gasgemischs und zugehöriges Reinigungsverfahren
EP3032203A1 (fr) 2014-12-09 2016-06-15 Linde Aktiengesellschaft Procédé et installation combinée destinés à stocker et à récupérer l'énergie

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KR20030046252A (ko) * 2001-12-05 2003-06-12 주식회사 포스코 공기분리장치의 한냉손실방지를 위한 운전방법
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