EP3594596A1 - Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant - Google Patents

Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant Download PDF

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Publication number
EP3594596A1
EP3594596A1 EP18020329.1A EP18020329A EP3594596A1 EP 3594596 A1 EP3594596 A1 EP 3594596A1 EP 18020329 A EP18020329 A EP 18020329A EP 3594596 A1 EP3594596 A1 EP 3594596A1
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EP
European Patent Office
Prior art keywords
heat exchange
exchange zone
operating mode
time
per unit
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Withdrawn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
EP18020329.1A
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German (de)
English (en)
Inventor
Reinhold Hölzl
Pascal Freko
Alexander WOITALKA
Patrick Haider
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Linde GmbH
Technische Universitaet Muenchen
Original Assignee
Linde GmbH
Technische Universitaet Muenchen
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by Linde GmbH, Technische Universitaet Muenchen filed Critical Linde GmbH
Priority to EP18020329.1A priority Critical patent/EP3594596A1/fr
Priority to PCT/EP2019/025222 priority patent/WO2020011396A1/fr
Publication of EP3594596A1 publication Critical patent/EP3594596A1/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Withdrawn legal-status Critical Current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
    • F25J3/04763—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
    • F25J3/04818—Start-up of the process
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0012—Primary atmospheric gases, e.g. air
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0247—Different modes, i.e. 'runs', of operation; Process control start-up of the process
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0248—Stopping of the process, e.g. defrosting or deriming, maintenance; Back-up mode or systems
    • 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
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
    • F25J1/0244—Operation; Control and regulation; Instrumentation
    • F25J1/0245—Different modes, i.e. 'runs', of operation; Process control
    • F25J1/0251—Intermittent or alternating process, so-called batch process, e.g. "peak-shaving"
    • 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
    • F25J3/04218—Parallel arrangement of the main heat exchange line in cores having different functions, e.g. in low pressure and high pressure cores
    • F25J3/04224—Cores associated with a liquefaction or refrigeration cycle
    • 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
    • F25J3/04333—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams
    • F25J3/04351—Generation of cold for compensating heat leaks or liquid production, e.g. by Joule-Thompson expansion using quasi-closed loop internal vapor compression refrigeration cycles, e.g. of intermediate or oxygen enriched (waste-)streams 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
    • F25J3/04763—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
    • 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
    • F25J2280/00—Control of the process or apparatus
    • F25J2280/10—Control for or during start-up and cooling down of the installation

Definitions

  • the invention relates to a method for operating a heat exchanger and an arrangement with a correspondingly operable heat exchanger according to the preambles of the respective independent claims.
  • Heat exchangers with cryogenic fluids i.e. Operate fluids at temperatures significantly below 0 ° C, in particular significantly below -100 ° C.
  • main heat exchangers also referred to as “main heat exchanger” or “main heat exchanger”
  • main heat exchanger of air separation plants
  • the present invention is also particularly suitable in systems for liquefying gaseous air products, for example gaseous nitrogen.
  • Corresponding plants can be supplied with gaseous nitrogen and liquefy it, in particular by air separation plants.
  • the liquefaction is not followed by a rectification like in an air separation plant. Therefore, when the problems described below are overcome, for example when there is no need for corresponding liquefaction products, these systems can be switched off completely and kept in standby until the next use.
  • the present invention therefore has as its object to provide measures which enable a corresponding heat exchanger to be put into operation again after a prolonged decommissioning without the disadvantageous effects mentioned.
  • the present invention proposes a method for operating a heat exchanger and an arrangement with a correspondingly operable heat exchanger, which can be designed in particular as an air processing system, system for storing and recovering electrical energy or system for liquefying an air product, with the features of respective independent claims. Refinements are the subject of the dependent claims and the following description.
  • a "heat exchanger” is an apparatus which is designed for the indirect transfer of heat between at least two fluid streams, for example in countercurrent to one another.
  • a heat exchanger for use in the context of the present invention can 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 only connected on the input and output sides via the respective headers. These are referred to below as “heat exchanger passages".
  • the terms “heat exchanger” and “heat (exchanger)” are used synonymously in the professional world. This also applies here.
  • the present invention relates in particular to the apparatuses designated as fin-plate heat exchangers in accordance with the German version of ISO 15547-2: 2005. If the term "heat exchanger” is used below, this should be understood to mean in particular a fin-plate heat exchanger.
  • a fin-plate heat exchanger has a large number of superimposed flat chambers or elongated channels, which are each separated from one another by corrugated or otherwise structured and interconnected, for example soldered plates, usually made of aluminum. The plates are stabilized by means of side bars and connected to each other. The structuring of the heat exchanger plates serves in particular to increase the heat exchange area, but also to increase the stability of the heat exchanger.
  • the invention relates in particular to brazed aluminum fin-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 and in plants for liquefying gaseous air products.
  • the storage and recovery of energy using liquid air is also referred to as Liquid Air Energy Storage (LAES).
  • LAES Liquid Air Energy Storage
  • a corresponding system is for example in the EP 3 032 203 A1 disclosed.
  • air is compressed, cooled, liquefied and stored in an insulated tank system in a first operating mode in a first operating mode.
  • the liquefied air stored in the tank system is heated in a second operating mode, in particular after a pressure increase by means of a pump, and thus converted into the gaseous or supercritical state.
  • a pressure stream obtained in this way is expanded in an expansion turbine which is coupled to a generator. The electrical energy obtained in the generator is fed back into an electrical network, for example.
  • cryogenic liquids formed using air can also be stored in the first operating mode and used to generate electrical energy in the second operating mode.
  • cryogenic liquids are liquid nitrogen or liquid oxygen or component mixtures which predominantly consist of liquid nitrogen or liquid oxygen.
  • external heat and fuel can also be coupled in in order to increase the efficiency and the output power, in particular using a gas turbine, the exhaust gas of which is expanded together with the pressure stream formed from the air product in the second operating mode.
  • the invention is also suitable for such systems.
  • Air separation plants can be used to provide appropriate cryogenic liquids. If liquid air is used, it is also possible to use pure air liquefaction systems.
  • air treatment plants is therefore also used below as a generic term for air separation plants and air liquefaction plants.
  • cold gas from a tank or exhaust gas from the stationary system can flow through a heat exchanger while the associated system is at a standstill, in order to avoid heating or to maintain the temperature profile formed.
  • a heat exchanger While the associated system is at a standstill, in order to avoid heating or to maintain the temperature profile formed.
  • such an operation can only be implemented with great effort in conventional methods.
  • the present invention proposes a method of operating a heat exchanger having a heat exchange zone extending between a first end and a second end, wherein in a first mode of operation fluids at different temperature levels are passed through the heat exchange zone in a first amount per unit time whereby the first end of the heat exchange zone is brought to a first temperature level and the second end of the heat exchange zone is brought to a second temperature level which is below the first temperature level.
  • a first operating mode corresponds to a normal operation of the heat exchanger, which is used for the temperature control of corresponding fluids, which can be provided in the form of one or more identical or different fluid flows.
  • At least one first fluid to be cooled is passed through the heat exchange zone from the first to the second end and at least one second fluid to be heated is passed from the second to the first end.
  • Corresponding temperature levels can in particular be at least partially in a cryogenic range.
  • the first temperature level can be in particular from 0 to 100 ° C, for example at approximately 20 ° C
  • the second temperature level can be in particular from -100 to 200 ° C, for example at approximately -175 ° C.
  • a corresponding heat exchanger can in particular also be “blocked in” completely, ie there is no longer any flow of fluid and any evaporating fluid that may be present is removed.
  • a corresponding heat exchanger can be arranged in a so-called cold box, in particular together with other apparatus.
  • a corresponding decommissioning can be particularly advantageous in the case of a plant for the liquefaction of a gaseous air product, for example gaseous nitrogen, since this is not connected to a rectification column system like an air separation plant.
  • the system switches repeatedly from the first operating mode to the second operating mode and from the second operating mode to the first operating mode.
  • Corresponding switching processes can in principle take place in different systems, but they are particularly important in systems in which an alternating mode of operation takes place routinely, for example systems for storing and recovering electrical energy using liquid air or other liquid air products.
  • the present invention is particularly advantageous in plants of this type. In principle, the present invention can be used in any system in which a heat exchanger can be operated accordingly.
  • these can be plants for liquefying natural gas and separating natural gas, the aforementioned LAES plants, plants for air separation, all types of liquefaction circuits (in particular for air and nitrogen) with and without air separation, ethylene plants (in particular separation plants that process gas mixtures) Steam crackers are set up), systems in which cooling circuits are used, for example with ethane or ethylene at different pressure levels, and systems in which carbon monoxide and / or carbon dioxide circuits are provided.
  • the switchover from the second operating mode to the first operating mode comprises the fluids which are conducted through the heat exchange zone in the first amount per unit time in the first operating mode, initially in a second amount until an increase in time per unit time, which is less than the first amount per unit time, to pass through the heat exchange zone and only to pass through the first heat exchange zone in the first quantity per unit time from the time of increase.
  • the switchover from the second operating mode can also take place in the form of a gradual or ramp-shaped transition. Even in such a case, the second quantity per unit of time (with the ramp-shaped increase) less than the first quantity per unit of time (after the increase). Ramps with different gradients, gradients with ramps and plateaus and the like can also be used. The same applies to a ramp-like increase after the time of the increase.
  • the present invention is based on the knowledge that the thermally induced voltages when restarting a heat exchanger, in particular a fin-plate heat exchanger from a temperature-balanced state, as can be present in particular after longer phases of an explained second operating mode, strongly depend on the speed of the restart can depend. While high mass flows can lead to high thermal voltages, the thermal stress can be significantly reduced at low start-up speeds with sufficiently small mass flows. More is particularly with reference to Figure 3 illustrated below.
  • the temperature profile when the apparatus starts up is set from the two ends as time progresses to the interior of the heat exchanger or its heat exchange zone. If the heat exchanger has already experienced the greatest temperature changes occurring during the transition to normal operation in sensitive areas, which are typically located in the terminal areas of a corresponding heat exchange zone, for example in a sensitive area of module connections, then only reduced gradients occur in the further course and thus reduced thermal stresses.
  • the present invention therefore proposes, with the measures mentioned above, first to pass fluids through the heat exchange zone with a smaller amount per unit of time and only afterwards, namely when the temperature change has already taken place sufficiently in appropriate sensitive areas, to increase or increase the amount to set a maximum amount.
  • the present invention enables, in particular, a significant service life optimization or improvement of fin-plate heat exchangers during restart processes from temperature-balanced conditions or at high temperature differences between incoming currents and metal temperatures of the Heat exchanger. Commissioning processes proposed according to the invention can in particular also be carried out for existing topologies (possibly by retrofitting surface temperature measurements or sensors and / or corresponding sensors at entry and / or exit points of the heat exchanger, in particular in connection with turbines), since the present invention essentially involves the optimization of the dynamic approach can be implemented.
  • the main heat exchangers of air separation plants can better withstand a load-flexible operating mode (for use, for example, electricity market prices) over the life of the plant through the use of the present invention. In this way, the present invention makes it possible to avoid unplanned downtimes, repair costs and procurement of spare parts.
  • the mode of operation of a corresponding system proposed according to the invention can be observed operationally, for example by means of surface temperature measurements.
  • the start-up process can thus be monitored and the time at which the start-up process can be accelerated can be well predicted.
  • a corresponding time of increase can therefore be determined in the context of the present invention at least in part on the basis of one or more temperature measurements at one or more points in the heat exchange zone. It is particularly advantageous here if such temperature measurements relate to a sensitive zone such as the aforementioned area of the module connection. However, other sensitive areas resulting from the design of the heat exchanger can also be taken into account within the scope of the present invention.
  • a corresponding area can be defined in particular via a longitudinal coordinate, which corresponds to the end of a module connection.
  • a measurement at another point is also possible in principle, provided that a temperature at a corresponding sensitive point can be inferred in this way, for example on the basis of known material properties and possibly model calculations with regard to heat spreading and fluid dynamics.
  • one or more surface temperature sensors can be used in the context of the present invention, which can be easily and inexpensively retrofitted in existing heat exchangers.
  • a corresponding heat exchanger is characterized with sufficient accuracy, for example with regard to material and thermal properties, and if the temperatures and fluid flows used are known, temperature measurement may also be dispensed with, because it can be assumed that after a certain time in the sensitive zones a corresponding temperature value has been reached. Therefore, as an alternative or in addition, it is also possible to base the increase in time at least in part on the basis of a period of time that has elapsed since the switchover was initiated and / or on the basis of the start of the supply of the fluids that are used in the second operating mode in the second quantity per unit time to set the elapsed period. For example, it is also possible to determine the switchover time on the basis of a total amount of the fluids which are used in the second operating mode in the second amount per unit of time.
  • the present invention unfolds its particular advantages when the heat exchanger is designed as a fin-plate heat exchanger.
  • a fin-plate heat exchanger can be made in particular of aluminum and / or stainless steel.
  • a corresponding heat exchanger can also be produced, for example, by means of 3D printing. In the case of such heat exchangers in particular, the potentially high thermal stresses mentioned may occur during repeated start-up processes.
  • the method according to the invention can be used particularly advantageously when the heat exchange zone has a first terminal partial zone extending from the first end, a second terminal partial zone extending from the second end and a central partial zone arranged between the first terminal partial zone and the second terminal partial zone , the point in time of the increase being determined as having been reached if it is established or predicted that one or more temperature values in at least one of the terminal sub-zones will exceed or fall below a predetermined temperature.
  • the heat exchanger can have a number of modules which are connected to one another by means of module connections, one or more of the module connections being or being arranged in the terminal sub-zones, and the central sub-zone being free of the module connections.
  • the invention permits targeted protection of the areas with the module connections or other sensitive zones, that is to say the first and second terminal sub-zones, which are particularly critical with regard to rapid temperature changes.
  • Module connections are particularly critical due to their notch effect, but the terminal end zones are fundamentally sensitive to thermally induced stresses, even if there is no module connection here. For details, please refer to the explanations above.
  • the point in time of the increase can in particular be determined to be reached when it is determined or predicted that one or more temperature values in at least one of the terminal sub-zones will exceed or fall below a predetermined temperature. More precisely, in such a case the time of increase can be determined as reached if it is determined or predicted that one or more temperature values in the first terminal sub-zones exceed a predetermined temperature and / or if it is determined or predicted that one or more temperature values in the fall below a predetermined temperature in the second terminal sub-zone.
  • switching from the second operating mode to the first operating mode may include an amount per unit time of the fluids that are conducted through the heat exchange zone in the first operating mode in the first amount per unit time to increase the time of increase continuously or gradually. In this way, temperature jumps can be further reduced.
  • one or more first fluids are fed to the heat exchange zone at its first end at the first temperature level, passed through the heat exchange zone and removed from the heat exchange zone at its second end at the second temperature level will or will, and that in the first operating mode one or more second fluids of the heat exchange zone at its second end at the second temperature level fed, passed through the heat exchange zone and the heat exchange zone at the first end or is removed at the first temperature level.
  • the present invention also extends to an arrangement having a heat exchanger which has a heat exchange zone which extends between a first end and a second end, and technical means are provided which are set up in a first operating mode to handle fluids at different temperature levels a first amount per unit time through the heat exchange zone, thereby bringing the first end of the heat exchange zone to a first temperature level and the second end of the heat exchange zone to a second temperature level which is below the first temperature level, with technical means being provided for this are configured, in a second operating mode, to at least partially prevent the passage of the fluids, which are passed through the heat exchange zone in the first amount per unit time in the first operating mode, as a result of which a temperature transition from the first end to the end is effected in the second end of the heat exchange zone, and technical means are provided which are set up to switch repeatedly in the method from the first operating mode to the second operating mode and from the second operating mode to the first operating mode.
  • the arrangement is characterized by technical means which are set up to carry out the switching from the second operating mode to the first operating mode in such a way that the fluids which are passed through the heat exchange zone in the first amount in the first quantity per unit time up to at a time of increase initially in a second amount per unit time, which is less than the first amount per unit time, are passed through the first heat exchange zone and are only passed through the first heat exchange zone in the first amount per time unit from the time of increase.
  • such a system has a control device which is designed to switch between the first and the second operating mode when required, for example according to a fixed switching pattern, on the basis of a sensor signal or on request.
  • a corresponding arrangement can in particular have suitable sensors, in particular temperature and / or strain sensors.
  • the present invention also extends to an arrangement which has means for the liquefaction and / or low-temperature separation of air and / or at least one gaseous air product.
  • this is characterized in that it represents an arrangement with a heat exchanger, as has just been explained.
  • the arrangement can be designed as an air separation plant.
  • it comprises a distillation column system of basically known type.
  • a corresponding arrangement can in particular also be designed as a system for storing and recovering energy.
  • a corresponding arrangement can also be designed as a plant for the liquefaction of nitrogen or as another plant of the type explained above.
  • Figure 1 illustrates temperatures in a heat exchanger, in particular a finned plate heat exchanger, after decommissioning, ie in an operating mode referred to above and below as "second operating mode", in which the passage of fluids through the heat exchanger is prevented, in the form of a temperature time diagram.
  • the temperature-time diagram shown are a temperature denoted by H at the warm end of the heat exchanger or its heat exchange zone (previously and hereinafter also referred to as "first end") and a temperature denoted by C at the cold end ("second end") in each case in ° C on the ordinate versus a time in hours on the abscissa.
  • the temperature H at the first (warm) end of the heat exchange zone at the beginning of the decommissioning and thus the temperature in a regular operation of the heat exchanger or at the end of the operating mode referred to above and below as the "first operating mode", in which corresponding fluids pass through the heat exchanger, about 20 ° C and the temperature C at the second (cold) end about -175 ° C.
  • the high thermal conductivity of the materials used in the heat exchanger is responsible for this. In other words, heat flows from the first (warm) end towards the second (cold) end. Together with the heat input from the environment, this results in an average temperature of approx. -90 ° C.
  • the significant temperature increase at the second (cold) end of the heat exchange zone is largely due to the internal temperature compensation in the heat exchanger and only to a lesser extent due to external heat input.
  • Figure 2 illustrates a fin-plate heat exchanger that can be operated using a method according to an embodiment of the invention. This is designated by a total of 100 and is fundamentally designed in a known manner, as documented, for example, in the specialist literature mentioned at the beginning.
  • the heat exchanger is designed for heat exchange between two fluids.
  • the present invention can in particular also be designed to operate corresponding heat exchangers in which more than two fluids are subjected to heat exchange.
  • the heat exchanger 100 is constructed from two modules 1, 2, which can in principle be configured identically. Instead of two modules 1, 2, heat exchangers with more than two modules can also be used within the scope of the present invention.
  • the modules 1, 2 are connected to one another by means of module connections, which, however, are only provided at the two ends of the two modules 1, 2.
  • the module connections 1, 2 can be designed, for example, as elements which are each soldered to the modules 1, 2.
  • the modules 1, 2, alternatively also a corresponding heat exchanger 100 as a whole, are each constructed from heat exchanger plates 4, of which only one is specifically designated in the example shown.
  • the heat exchanger plates 4 can in particular be soldered to one another. In particular, they are combined alternately in groups, which can be flowed through separately.
  • the two modules 1, 2 can be supplied with a warm or a cold fluid via headers 5 and 7, respectively. Corresponding fluids are fed into the respective headers by means of connecting pieces 51 and 71. A warm fluid is distributed by means of the header 5 to a group of heat exchanger plates 4 of the modules 1, 2.
  • a cold fluid is distributed to another group of heat exchanger plates 4 of the modules 1, 2 by means of the header 7.
  • a corresponding heat exchanger 100 can also be set up to process further fluid flows.
  • Corresponding groups of heat exchanger plates 4 and headers are provided for this.
  • a heat exchange zone 10 of the heat exchanger 100 For heat exchange, corresponding fluids flow through a heat exchange zone 10 of the heat exchanger 100, designated here as 10, which extends between a first end, here designated 11, and a second end, designated here 12.
  • first regular
  • first fluids at different temperature levels are passed through the heat exchange zone 10 in a specific (“first”) amount per unit of time in the manner previously explained.
  • first the first end 11 of the heat exchange zone 10 is brought to a certain (“first") temperature level and the second end 12 of the heat exchange zone 10 is also brought to a certain ("second”) temperature level which is below the first temperature level.
  • the heat exchanger 100 shown here is characterized in particular by the fact that the heat exchange zone 10 has a first terminal sub-zone 13 extending from the first end 11 and a second terminal sub-zone 14 extending from the second end 12 and in the terminal sub-zones 13, 14 each of the module connections 3 are arranged.
  • a central subzone of the heat exchange zone 10, however, is free of the module connections 3.
  • Figure 3 illustrates a relationship between fluid flows and thermal stresses in a fin-plate heat exchanger.
  • Figure 3 are a normalized cold mass flow in dimensionless units, i.e. a quantity of a cold fluid supplied to the heat exchanger per unit time, on the abscissa and a normalized maximum thermal stress in dimensionless units on the ordinate.
  • the thermal stresses induced at low mass flows are significantly lower than at higher mass flows.
  • the present invention makes use of this knowledge and, in particular, proposes to start up a corresponding heat exchanger again using smaller amounts of fluid per unit of time.
  • an amount of fluid is only increased when the areas in which module connections of a finned plate heat exchanger constructed from several modules, for example a heat exchanger as shown in Figure 2 shown, are arranged, are already sufficiently temperature-controlled, since there are particularly negative effects of the thermal stresses in such areas. This is with reference to Figure 4 further explained.
  • the present invention proposes to switch from the second operating mode to the first operating mode in such a way that the fluids which are conducted in the first operating mode in the first quantity per unit time through the heat exchange zone of a corresponding heat exchanger up to an increase time first in a second quantity per unit time, which is less than the first quantity per unit time, to pass through the first heat exchange zone and only from the time of increase in the first quantity per unit time through the first heat exchange zone.
  • the temperature profile when starting that is, from the transition from the second to the first operating mode, from the two ends starting with progressive time to the interior of the heat exchanger or the heat exchange zone, is set. If the heat exchanger, for example in a sensitive area of module connections, has already experienced the greatest temperature changes occurring during the transition to the first operating mode, then only reduced gradients and thus greatly reduced thermal voltages then occur in the further course. In the context of the present invention, the temperature changes of corresponding sensitive areas are brought about in particular with reduced amounts of fluid. Only then is a corresponding heat exchanger operated with the full amount of fluid.
  • Diagrams 410 to 460 are each shown, in each of which temperature profiles 401 to 406 in a heat exchange zone of a heat exchanger, for example of the heat exchanger 100 according to FIG Figure 2 shown at different times. The times are each after a point in time at which a balanced temperature profile has been established due to a heat transfer from the warm to the cold end because the fluid supply has been cut off, that is to say after some time in the second operating mode.
  • the heat exchange zone and its partial zones are also designated here in the diagram 410 with 10, 13 and 14.
  • corresponding thermal voltages are reduced, in particular, by using lower mass flows in a targeted manner in the periods in which the areas of the module connections experience large temperature changes (corresponding to diagrams 410 to 440).
  • Has the local temperature gradient already formed over the module connections (corresponding to diagram 550) the approach speed can be accelerated again if necessary and thus based on common procedures without generating any further significant voltage peaks.
  • Figure 5 is a nitrogen liquefaction plant that can be operated using a method according to an embodiment of the invention, is schematically illustrated and is designated overall by 500.
  • the illustrated system 500 has, in particular, a heat exchanger 100 of the type explained above or a comparable heat exchanger. Plants for nitrogen liquefaction are known in principle and are not restricted to the exemplary embodiment shown.
  • plant 500 is supplied with gaseous nitrogen (stream a), which can be provided, for example, by means of an air separation plant.
  • the gaseous nitrogen is fed to a multi-stage compressor 510 and compressed.
  • a portion of the compressed gaseous nitrogen (stream b) is further compressed in turbine boosters 520, 530, which are each provided with aftercoolers, and fed to the heat exchanger 100 on the warm side.
  • the rest (stream c) remains undensified and is also fed to the heat exchanger 100 on the warm side.
  • a partial flow d of the flow b is taken from the heat exchanger 100 at an intermediate temperature level, expanded in a relaxation turbine of the turbine booster 520 and fed into a container 540.
  • Another partial stream e of stream c is taken from the heat exchanger 100 on the cold side and expanded into the tank 540 via a throttle (not specifically designated).
  • the stream c is taken from the heat exchanger 100 at an intermediate temperature level, expanded in a expansion turbine of the turbine booster 530, fed to the heat exchanger 100 at an intermediate temperature level and returned together with gaseous nitrogen from the container 540 as stream f to the compressor 510 at an intermediate pressure level.
  • Liquid nitrogen from the container 540 is subcooled in a subcooler 550, which is cooled with a part of this nitrogen (stream g), and expanded into a storage tank 560 as stream h. Due to evaporation, gaseous nitrogen is now formed in the storage tank 560 and can be discharged unused as current i via a line and a valve if required. In addition, when the liquid nitrogen is transported from the subcooler 550 via the corresponding line (stream h) into the storage tank 200, flash gas is formed, which is also undesirable.
  • a further line can now be provided, via which gaseous and cold nitrogen can be fed back from the storage tank 560 as stream k into the liquefaction process.
  • this gaseous nitrogen is combined with the stream g upstream of the subcooler 550.
  • a current I formed by combining the currents g and k can also be returned to the current a after heating, i.e. the amount of gaseous nitrogen carried in stream k is fed via stream I to stream a and thus again to the liquefaction process.
  • the system 500 can, if the measures proposed according to the invention are implemented, be switched on and off as required, depending on the need for liquid nitrogen.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Mechanical Engineering (AREA)
  • Thermal Sciences (AREA)
  • General Engineering & Computer Science (AREA)
  • Separation By Low-Temperature Treatments (AREA)
EP18020329.1A 2018-07-13 2018-07-13 Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant Withdrawn EP3594596A1 (fr)

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EP18020329.1A EP3594596A1 (fr) 2018-07-13 2018-07-13 Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant
PCT/EP2019/025222 WO2020011396A1 (fr) 2018-07-13 2019-07-11 Procédé destiné à faire fonctionner un échangeur de chaleur, système pourvu d'un échangeur de chaleur et installation de traitement d'air pourvue d'un système correspondant

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EP18020329.1A EP3594596A1 (fr) 2018-07-13 2018-07-13 Procédé de fonctionnement d'un échangeur de chaleur, système comprenant un échangeur de chaleur et installation de traitement d'air dotée d'un système correspondant

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WO2022208003A1 (fr) * 2021-04-01 2022-10-06 Gaztransport Et Technigaz Procédé de refroidissement d'un échangeur thermique d'un système d'alimentation en gaz d'un appareil consommateur de gaz d'un navire
EP4246070A1 (fr) 2022-08-31 2023-09-20 Linde GmbH Procédé et installation de liquéfaction de gaz

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Publication number Priority date Publication date Assignee Title
WO2022208003A1 (fr) * 2021-04-01 2022-10-06 Gaztransport Et Technigaz Procédé de refroidissement d'un échangeur thermique d'un système d'alimentation en gaz d'un appareil consommateur de gaz d'un navire
FR3121504A1 (fr) * 2021-04-01 2022-10-07 Gaztransport Et Technigaz Procédé de refroidissement d’un échangeur thermique d’un système d’alimentation en gaz d’un appareil consommateur de gaz d’un navire
EP4246070A1 (fr) 2022-08-31 2023-09-20 Linde GmbH Procédé et installation de liquéfaction de gaz

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