EP3557165A1 - Procédé de fonctionnement d'un échangeur thermique, système doté d'un échangeur thermique et installation d'alimentation en air dotée d'un tel système - Google Patents

Procédé de fonctionnement d'un échangeur thermique, système doté d'un échangeur thermique et installation d'alimentation en air dotée d'un tel système Download PDF

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Publication number
EP3557165A1
EP3557165A1 EP18020163.4A EP18020163A EP3557165A1 EP 3557165 A1 EP3557165 A1 EP 3557165A1 EP 18020163 A EP18020163 A EP 18020163A EP 3557165 A1 EP3557165 A1 EP 3557165A1
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EP
European Patent Office
Prior art keywords
exchange zone
zone
temperature level
operating mode
exchange
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Withdrawn
Application number
EP18020163.4A
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German (de)
English (en)
Inventor
Lars Kirchner
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Linde GmbH
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Linde GmbH
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Publication date
Application filed by Linde GmbH filed Critical Linde GmbH
Priority to EP18020163.4A priority Critical patent/EP3557165A1/fr
Priority to PCT/EP2019/025097 priority patent/WO2019201475A1/fr
Publication of EP3557165A1 publication Critical patent/EP3557165A1/fr
Withdrawn legal-status Critical Current

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    • 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 preambles of the respective independent claims.
  • 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 in principle it is also suitable for use in other fields of application, for example systems for storing and recovering energy using liquid air or natural gas liquefaction.
  • the temperature profiles at standstill of the associated system is then fed, for example, when restarting in a heated part of the heat exchanger cryogenic gas or vice versa warm gas in a cooled part of the heat exchanger, it comes to high thermal stresses cause damage to the heat exchanger or require a disproportionately high material or manufacturing costs.
  • the present invention therefore has as its object to provide measures that allow re-commissioning of a corresponding heat exchanger after prolonged shutdown without the aforementioned adverse effects.
  • the present invention proposes a method for operating a heat exchanger and an arrangement with a correspondingly operable heat exchanger, which may be designed in particular as an air handling unit, with the features of the respective independent claims.
  • a “heat exchanger”, as used herein, is an apparatus capable of indirectly transferring heat between at least two e.g. is formed in countercurrent to each other guided fluid flows.
  • a heat exchanger for use in the present invention may be formed of a single or multiple heat exchanger sections connected in parallel and / or in series, e.g. 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 of superposed flat chambers or elongate channels, each through corrugated or otherwise structured and interconnected, for example, soldered plates, i.d.R. made of aluminum, are separated from each other. 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.
  • the storage and recovery of energy using liquid air is described in English also known as Liquid Air Energy Storage (LAES).
  • LAES Liquid Air Energy Storage
  • a corresponding plant is for example in the EP 3 032 203 A1 disclosed.
  • 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 obtained in the generator is, for example, fed back into an electrical network.
  • a corresponding storage and recovery of energy is basically not only possible using liquid air. Rather, in the first mode of operation, other cryogenic liquids formed using air may be stored and used in the second mode of operation to generate electrical energy. Examples of corresponding cryogenic liquids are liquid nitrogen or liquid oxygen or component mixtures which consist 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. Also for such systems, the invention is suitable.
  • air separation plants can serve to provide the corresponding cryogenic liquids. 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 processing plants” is therefore used below.
  • 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.
  • 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.
  • such an operation is possibly only expensive to implement in conventional methods.
  • 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 type 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 respectively define areas of separate heat exchange, that is to say the "exchange areas" of the previously explained type.
  • each part or individual heat exchanger results in a decommissioning also a temperature balance 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 correspondingly formed heat exchanger does not extend from the highest to the lowest temperature level of the total heat exchanger, but only up to or from an intermediate temperature level, which is present at the separation point between the parts or individual heat exchangers , can be achieved by a heat conduction within the respective part or individual heat exchanger initially only a mean temperature level, which is between the temperature level at the warm end and the intermediate temperature level on the one hand and between the intermediate temperature level and the temperature level at the other.
  • This average temperature level is higher in a part or individual 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 Exchange zone, the first end of the first exchange zone is heated to a first temperature level and the second end of the second exchange zone is heated to a second temperature level below the first temperature level.
  • 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.
  • 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 first operating mode is interrupted by a second operating mode in which the passage of fluid through the first exchange zone and the second exchange zone is prevented.
  • 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.
  • 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 first exchange zone can be at a subsequent re-commissioning with a warm fluid at the first temperature level and the second exchange zone with a cold fluid at the second temperature level are applied, without in each case can lead to excessively high thermal stresses as in a conventional formation of a compensation temperature level in the heat exchanger as a whole.
  • 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 of the second exchange zone carried heat transfer after the initiation of the second operating mode indicates a predetermined value exceeds or falls below.
  • the variable characterizing the heat transfer which has taken place can in particular be a temperature at the first end of the first or the second end of the second exchange zone. This can be determined in particular by means of a measurement in the form of one or more temperature values. However, it may also be provided to use a time control.
  • 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. This is also a time corresponding to a size that characterizes a 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 operating mode.
  • a corresponding time specification can be applied, for example on the basis of established initial temperatures, with correction factors or surcharges and discounts.
  • 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 exchange zone and / or between the first end and the second end of the second Exchange zone characterized heat transport after the initiation of the second operating mode indicates a predetermined value exceeds or falls short of can be ensured that the temperatures at the warm end of a corresponding heat exchanger have not fallen so low that a supply of fluid at the warm end can lead to excessive temperature stresses. The same applies to the temperatures at the cold end of a corresponding heat exchanger.
  • corresponding values for example threshold values or time specifications, can be selected in such a way that it is ensured that, if necessary, a temperature within the first and the second heat exchange zone is equalized, a temperature compensation in the heat exchanger has not yet taken place overall.
  • 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.
  • 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 carried out heat transport after the initiation of the second mode of operation indicates the predetermined value is above or below.
  • a corresponding further operating mode may in particular also be a tempering mode in which the heat exchanger is tempered by measures known per se. In this case, in particular, a flow through a corresponding heat exchanger with Fluid flows take place, which can be used in a smaller amount per unit time than the fluid streams used in the first operating mode.
  • 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 second operating mode can be interrupted and the first operating mode or the further operating mode can be initiated as soon as the first end of the first exchange zone has a temperature level which deviates from the first temperature level by more than a predetermined value and / or as soon as the second end of the first second exchange zone has a temperature level which differs by more than a predetermined value from the second temperature level.
  • the second end of the first exchange zone and the first end of the second exchange zone by passing fluids through the first exchange zone and through the second exchange zone to a third intermediate temperature level between the first temperature level and the second temperature mode are then tempered, the second operating mode is then interrupted and the first operating mode or the further operating mode are initiated as soon as the first end of the first exchange zone has a temperature level which is more than a predetermined value from a mean temperature level between the first temperature level and deviates from the third temperature level and / or as soon as the second end of the second exchange zone has a temperature level which is more than a predetermined value from a mean temperature level between the third temperature level and the second temperature level deviates.
  • one or more first fluids are or are supplied in particular at the first temperature level of the first exchange zone via the first end thereof, successively passing through the first exchange zone, the separation zone and the second exchange zone, and thereafter at the second temperature level from the second exchange zone via the second end thereof
  • one or more second fluids are or will be successively at the second temperature level supplied second exchange zone via the second end thereof, passed through the second exchange zone, the separation zone and the first exchange zone, and thereafter carried out at the first temperature level from the first exchange zone via the first end thereof.
  • the temperature of the first and the second heat exchange zone is carried out in the manner explained in more detail above, wherein set at the second end of the first and at the first end of the second heat exchange zone, a further temperature level which is between the first and the second temperature level ,
  • 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 comprise one or more first materials having one or more 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).
  • 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.
  • the first exchange zone and the second exchange zone can be formed in any desired 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 is at least partially filled with an insulating material, 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 each have superimposed metal plates with a first structuring
  • first structuring and for the separation zone to have superimposed metal plates with a second structuring that deviates from the first structuring.
  • 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 heat exchanger having a first exchange zone with a first end and a second end, a second exchange zone with a first end and a second end and a separation zone between the first end of the first exchange zone and the 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 thereof 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.
  • technical means are provided which are set up to temper the first end of the first exchange zone to a first temperature level in a first operating mode by passing fluids through the first exchange zone and through the second exchange zone and tempering the second end of the second exchange zone to a second temperature level below the first temperature level. 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 fluid 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 to interrupt the second operating mode and to initiate the first operating mode or another operating mode 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 of the second exchange zone heat transfer after the initiation of the second mode of operation is characterized, exceeds or falls below a predetermined value.
  • 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 request to switch between the first and the second operating mode.
  • the present invention also extends to an air handling plant having means for liquefying and / or cryogenic separation of air.
  • the air processing plant can 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. 10 illustrates temperature profiles in a heat exchanger after decommissioning without the use of measures according to an embodiment of the present invention.
  • FIG. 2 FIG. 10 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 after decommissioning without the use of measures according to advantageous embodiments of the present invention in the form of a temperature diagram.
  • FIG. 2 illustrates temperature profiles in a heat exchanger after decommissioning without the use of measures according to advantageous embodiments of the present invention in the form of a temperature diagram.
  • FIG. 1 The diagram shown is a temperature designated H at the warm end of a corresponding heat exchanger or its corresponding heat exchange area (previously and subsequently also referred to as "first end") and a temperature designated C at the cold end (previously and subsequently as “second end” respectively) in ° C on the ordinate versus time in hours on the abscissa.
  • the temperature is H at the first (warm) end of the heat exchange area at the start of decommissioning, and thus the 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. Together with the heat input from the environment results in an average temperature of about -90 ° C.
  • the significant increase in temperature at the second (cold) end of the heat exchange area is largely due to the internal temperature compensation in the heat exchanger and only to a lesser extent by external heat input.
  • FIG. 2 illustrates an air separation plant as an example of an arrangement 100 according to an embodiment of the present invention. This has as essential components a heat exchanger 10, which is the main heat exchanger of the air separation plant, and a distillation column system 20.
  • 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 , in particular 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 on the embodiment according to FIG. 2 limited. FIG. 2 only illustrates the components essential to the description of the present invention.
  • the heat exchanger 10 comprises a first exchange zone, designated here by 1, having a first end 11 and a second end 12 and a second exchange zone, designated here by 2, having a first end 21 and a second end 22.
  • a separating zone, designated here by 3 is present the first end 11 of the first exchange zone 1 and the second end 12 of the second exchange zone 2 is formed.
  • 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 11 and the second end 12 and a thermal conductivity of the second exchange zone 2 between the first end 11 and the second end 12 is higher than a thermal conductivity of the separation zone 13 between the second end 11 of 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 explained below, by passing fluids through the first exchange zone 1 and through the second exchange zone 2, the first end 11 of the first exchange zone 1 is at a first temperature level and the second end 12 of the second exchange zone 2 is 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 to the first exchange zone 1 via its first end 11, successively passed through the first exchange zone 1, the separation zone 3 and the second exchange zone 2, and then carried out at the second temperature level from the second exchange zone 2 via the second end 22 thereof.
  • 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 stream 102 is fed in the example shown after its expansion in the expansion device 30 in a low-pressure column 22 of the distillation column system 20.
  • the high-pressure column 21 and the low-pressure column 22 are in a known manner with each other via a main capacitor 23 in heat exchanging connection.
  • 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.
  • 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 stream of material 106 is withdrawn.
  • the stream 106 is passed through the subcooling countercurrent 34.
  • the material streams 105 and 106 are supplied sequentially at the second temperature level of the second exchange zone 2 of the heat exchanger 10 via the second end 22, passed through the second exchange zone 2, the separation zone 3 and the first exchange zone 1, and thereafter at the first temperature level of the first Exchange zone 1 executed on the first end 11.
  • 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 size that characterizes a heat transfer 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 of the second exchange zone 2 after the initiation of the second operating mode, as explained in more detail a exceeds or falls below the predetermined value.
  • one or more temperature sensors 40 can be used to determine a corresponding value.

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  • Engineering & Computer Science (AREA)
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  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Health & Medical Sciences (AREA)
  • Emergency Medicine (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP18020163.4A 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 Withdrawn EP3557165A1 (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
PCT/EP2019/025097 WO2019201475A1 (fr) 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

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EP4055335A4 (fr) * 2019-11-07 2024-06-05 ConocoPhillips Company Systèmes et procédés d'élimination de l'azote pendant la liquéfaction de gaz naturel

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