WO2020011396A1 - 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 - Google Patents

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 Download PDF

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Publication number
WO2020011396A1
WO2020011396A1 PCT/EP2019/025222 EP2019025222W WO2020011396A1 WO 2020011396 A1 WO2020011396 A1 WO 2020011396A1 EP 2019025222 W EP2019025222 W EP 2019025222W WO 2020011396 A1 WO2020011396 A1 WO 2020011396A1
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Prior art keywords
heat exchange
exchange zone
operating mode
time
heat exchanger
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PCT/EP2019/025222
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German (de)
English (en)
Inventor
Reinhold Hölzl
Pascal Freko
Alexander WOITALKA
Patrick Haider
Original Assignee
Linde Aktiengesellschaft
Technische Universität München
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Application filed by Linde Aktiengesellschaft, Technische Universität München filed Critical Linde Aktiengesellschaft
Publication of WO2020011396A1 publication Critical patent/WO2020011396A1/fr

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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
    • F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
    • F25J3/04763—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 exchangers” or “main heat exchangers” of air separation plants, but in principle it is also suitable for use in others
  • heat exchanger is used routinely, even if strictly speaking no “exchange” of heat takes place in such an apparatus.
  • 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 like in a
  • Air separation plant a rectification downstream. 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.
  • Air separation plants and other heat exchangers flowed through with warm and cryogenic media when the associated plant and thus the
  • the heat exchanger only warms up to the ambient temperature over a much longer period.
  • This case relates to the present invention. This behavior is observed in particular when the main heat exchanger, which is housed in a cold-insulated manner, is blocked together with the rectification unit when an air separation plant is switched off, ie when no more gas is supplied from the outside. In such a case, typically only gas that is produced due to thermal insulation losses is blown off cold.
  • a system for liquefying a gaseous air product for example liquid nitrogen
  • US 2002/017468 A1, US 3,469,271 A and DE 10 2009 042994 A1 also relate to methods for operating heat exchangers or corresponding arrangements with heat exchangers.
  • the present invention therefore has as its object to provide measures which require certain heat exchangers to be restarted after a prolonged period
  • the present invention proposes a method for operating a heat exchanger and an arrangement with a correspondingly operable Heat exchanger, in particular as an air treatment plant, plant for storing and recovering electrical energy or plant for
  • a “heat exchanger” in the parlance used here is an apparatus which is used for the indirect transfer of heat between at least two e.g. fluid flows guided in countercurrent to one another.
  • a heat exchanger for use in the present invention may be formed from a single or a plurality of 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 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 often used synonymously in the professional world. This also applies here.
  • the present invention relates to the apparatus referred to as plate fin heat exchangers in accordance with the German version of ISO 15547-2: 2005. If the term "heat exchanger” is used below, it is understood to mean a fin-plate heat exchanger. A finned plate heat exchanger has a plurality of superimposed flat
  • Chambers or elongated channels which are each separated 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 disclosed, for example, in EP 3 032 203 A1.
  • Liquids are stored and used in the second operating mode for the generation of electrical energy. Examples of corresponding cryogenic
  • Liquids are liquid nitrogen or liquid oxygen or
  • Component mixtures consisting mainly 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 are used. If liquid air is used, it is also possible to use pure air liquefaction systems. As a generic term for Air separation plants and air liquefaction plants, the term “air treatment plants” is therefore also used below.
  • a heat exchanger can be flowed through with cold gas from a tank or exhaust gas from the stationary system during a standstill of the associated system in order to avoid heating or the developed one
  • the process may only be complex to implement.
  • Flow velocities in the heat exchanger can result in an incorrect distribution within a heat exchanger block and in particular over several
  • Heat exchanger blocks cannot be excluded. In principle, however, it is desirable to keep the amounts of gas used low in order to
  • cryogenic media For example, to avoid product losses or the consumption of appropriate cryogenic media. Furthermore, implementation is more appropriate
  • the present invention proposes a method for operating a
  • Heat exchanger which has a heat exchange zone, which extends between a first end and a second end, and which has a plate stack of heat transfer plates, the heat transfer plates, as is customary in this regard for fin-plate heat exchangers, structured (profiled, corrugated and, if necessary have perforated) sheets and corresponding edge bars (English sidebars).
  • a parallelepiped-shaped block is formed by a corresponding plate stack, which block has corresponding headers for feeding and removing fluids, as is common practice.
  • the heat exchanger operated according to the invention is, as mentioned, a fin-plate heat exchanger of a known type.
  • the present invention is applied to a heat exchanger in which a width of the heat transfer plates and a height of that formed therefrom
  • Plate stacks in the heat exchange zone between one fifth and one each Is a third of the length of the heat transfer plates between the first end and the second end.
  • the width of the heat transfer plates is a dimension in a direction that is perpendicular to a main flow direction of the fluids through the heat exchanger or orthogonal to a shortest connection between the first and the second end and in a plane of the respective heat exchanger plates.
  • the stack height denotes the added heights of the respective
  • Heat exchanger plates perpendicular to their plane.
  • the present invention thus already differs in this point from known methods for operating wound heat exchangers.
  • a wound heat exchanger completely different temperature compensation phenomena occur than in a finned plate heat exchanger, because here the wound ones
  • Heat exchanger tubes or capillaries are also subjected to heat exchange with adjacent tubes or capillaries, but primarily with the surrounding jacket space, in which a gaseous medium to be heated typically flows.
  • Heat exchangers present overall in a smaller proportion and in particular less rigid material transitions can be exposed to this, if necessary, significantly harsher temperature gradients. It is therefore not obvious to transfer suitable measures for a wound heat exchanger to a fin-plate heat exchanger. The specialist would have been prevented by the fundamentally different boundary conditions here.
  • Temperature distribution over the entire cross-sectional area of the heat exchanger can adjust. In other words, even with reduced fluid feed, this can result in any cross-sectional plane between the first end and the second In the end, a temperature distribution can be achieved in which a maximum temperature and a minimum temperature do not differ by more than 20, 10 or 5 K.
  • the present invention proposes that, in a first operating mode, fluids are provided at different feed temperature levels and are each passed through the heat exchange zone in a first quantity per unit of time, 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 second temperature level, which is in particular below the first temperature level, is brought.
  • the feed temperature levels are those at which the corresponding fluids are also fed into the heat exchanger or are fed to the heat exchanger at the first or second end. They comprise a first feed temperature level of a fluid to be cooled and a second feed temperature level of a fluid to be heated, the first feed temperature level in the case of an air separation plant in particular at ambient temperature or at 0 to 30 ° C. and the second
  • the first temperature level, to which the first end of the heat exchange zone is brought, and the second temperature level, to which the second end of the heat exchange zone is brought, result in particular from the feed temperature levels mentioned. They are close to these, i.e. in particular, they reject them by no more than 20 ° C. or no more than 10 ° C.
  • Such a first operating mode corresponds to 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. So the first temperature level in particular at 0 to 100 ° C, for example at about 20 ° C and the second temperature level in particular at -100 to -200 ° C, for example at about -175 ° C.
  • 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.
  • Heat exchange zone at the first end of the heat exchange zone set a third temperature level and at the second end of the heat exchange zone a fourth temperature level.
  • the temperature level in the case considered in the context of the present invention is always greater than a difference between the third
  • Temperature level and the fourth temperature level In the second operating mode, therefore, a certain temperature compensation occurs, which can also have the effect that the third and fourth temperature levels are the same or at least do not differ by more than 50, 40, 30, 20 or 10 K.
  • the invention does not relate to the fully heated state of a corresponding heat exchanger.
  • an average value between the third temperature level and the fourth temperature level does not deviate by more than 50, 40, 30, 20 or 10 K from an average value between the first temperature level and the second temperature level.
  • the two mean values are therefore similar or the same and differ only because of a temperature input (which is significantly slower than the heat balance between the warm and the cold end).
  • a temperature difference between the first and the second temperature level can be more than 150 K in particular.
  • the mean value between the third and fourth, and thus also between the first and the second temperature level deviates in particular by more than 50 K and up to 100 K from the closest feed-in temperature level (which may be above or below) ,
  • 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.
  • the present invention can be used in any system in which a heat exchanger can be operated accordingly.
  • plants for liquefaction and separation of natural gas the aforementioned LAES plants, plants for air separation,
  • Liquefaction circuits of all kinds especially for air and nitrogen
  • ethylene plants in particular separation plants that are set up to process gas mixtures from steamer racks
  • Cooling circuits for example with ethane or ethylene on different
  • Pressure levels are used and systems in which carbon monoxide and / or carbon dioxide cycles are provided act.
  • the switchover from the second operating mode to the first operating mode includes the fluids that flow through the first amount per unit time in the first operating mode
  • Heat exchange zone are to be conducted through the heat exchange zone in a second quantity per unit of time, which is less than the first quantity per unit of time, until a point in time of elevation and only through the first heat exchange zone in the first quantity per unit of 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) is 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 in a suitable manner
  • temperature-balanced state as may be present in particular after longer phases of an explained second operating mode, can strongly depend on the speed of the restart. 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 below with reference to Figure 3
  • the present invention exerts its effects in the heat exchangers explained above, since here a sufficiently balanced temperature profile can also be achieved in cross-section through the heat exchange zone by means of a sufficiently fast cross conduction.
  • the temperature profile at Starting of the apparatus from the two ends starting with progressive time to the interior of the heat exchanger or its heat exchange zone.
  • 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, the heat exchanger already has the largest areas occurring during the transition to normal operation
  • the invention therefore proposes, with the above-mentioned measures, first to guide fluids through the heat exchange zone with a smaller amount per unit of time and only afterwards, namely to increase the amount or to increase the amount, if the temperature has already changed sufficiently in corresponding sensitive areas set maximum amount.
  • the present invention enables 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.
  • the main heat exchangers of air separation plants can be operated in a load-flexible manner (for
  • 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.
  • the corresponding area can be defined in particular by means of a longitudinal coordinate which corresponds to the end of a module connection.
  • a measurement at another location is also possible in principle, provided that a temperature at a corresponding sensitive location can be inferred in this way, for example on the basis of known material properties and possibly
  • Is a corresponding heat exchanger for example, characterized with sufficient accuracy with regard to material and thermal properties, and are
  • Temperature measurement can be dispensed with, because it can be assumed that after a certain time in the sensitive zones, a corresponding one
  • Temperature value is 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. It is also possible, for example, to base the switchover time on a
  • 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 for example, be produced by means of 3D printing. Especially with such
  • Heat exchangers may experience the mentioned potentially high thermal stresses 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 has, the
  • the point in time of the increase is 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.
  • 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. Due to the slow approach, the present invention permits targeted protection of the areas with the module connections or other sensitive zones, that is to say the first and second terminal partial zones, which are particularly critical with regard to rapid temperature changes. Module connections are particularly due to their
  • 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 the increase can be defined 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-zones.
  • the changeover between the first and the second quantity per unit of time can take place suddenly or gradually.
  • 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 the
  • 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 is or will be, and that in the first mode of operation one or more second fluids are supplied to the heat exchange zone at its second end at the second temperature level, passed through the heat exchange zone and removed from the heat exchange zone at its first end at the first temperature level.
  • the present invention also extends to an arrangement with a
  • Heat exchanger which has a heat exchange zone which extends between a first end and a second end and which has a plate stack of heat transfer plates, wherein a width of the
  • Heat exchange zone each a fifth to a third of a length of the
  • Heat transfer plates between the first end and the second end are provided. According to the present invention, technical means are provided which are set up to operate different fluids in a first operating mode
  • Feed temperature levels are provided and each in a first amount per unit of time through the heat exchange zone, whereby 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 in particular below the first temperature level, whereby technical Means are provided which are set up to operate the in a second operating mode
  • Heat exchange zone sets a third temperature level at the first end of the heat exchange zone and a fourth temperature level at the second end of the heat exchange zone, with a difference between the first
  • Temperature level and the second temperature level is greater than a difference between the third temperature level and the fourth temperature level and an average value between the third temperature level and the fourth temperature level does not deviate by more than 50 K from an average value between the first temperature level and the second temperature level.
  • the invention provides that technical means are provided which are set up to switch several times 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 each case in the first quantity per unit of time at a time of increase, are first passed through the first heat exchange zone in a second amount per time unit, which is less than the first amount per time unit, 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, if necessary, for example according to a fixed switching pattern, on the basis of a sensor signal or
  • 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. According to the invention, 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. In this case, it comprises a distillation column system
  • 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 temperature profiles at the warning and cold end of a heat exchanger operable according to the invention after decommissioning.
  • Figure 2 illustrates a finned plate heat exchanger that can be operated using a method according to an embodiment of the invention.
  • Figure 3 illustrates a relationship between fluid flows and thermal stresses in a fin-plate heat exchanger.
  • Figure 4 illustrates temperature gradients in a fin-plate heat exchanger at different times of flow.
  • FIG. 5 illustrates a nitrogen liquefaction plant that can be operated using a method according to an embodiment of the invention
  • elements that are identical or correspond to one another functionally or in terms of meaning are given identical reference numerals and are not explained repeatedly for the sake of clarity.
  • Figure 1 illustrates temperatures in a heat exchanger, particularly a finned plate heat exchanger, after decommissioning, i.e. in a previously and subsequently also referred to as "second operating mode" operating mode, in which the passage of fluids through the heat exchanger is prevented, in the form of a temperature-time diagram.
  • second operating mode operating mode
  • the temperature-time diagram shown in FIG. 1 shows a temperature denoted by H (also referred to here as “first temperature level”) at the warm end of the heat exchanger or its heat exchange zone ("first end") and a temperature denoted by C ( “second temperature level”) at the cold end ("second end”) each in ° C on the ordinate versus a time in hours on the abscissa.
  • H also referred to here as "first temperature level”
  • C cold end
  • the temperature H at the first (warm) end of the heat exchange zone at the beginning of the decommissioning, and thus the temperature during 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 the corresponding fluid is passed through the heat exchanger, approx. 20 ° C and the temperature C at the second (cold) end approx. -175 ° C.
  • These temperatures become increasingly similar over time.
  • 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 a
  • Temperature level at the second end (“fourth temperature level") and 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 one
  • Tensions arise when the first (warm) end of the heat exchanger is again exposed to a warm fluid of approximately 20 ° C. in the example shown after some time in the second operating mode.
  • FIG. 2 illustrates a fin-plate heat exchanger which can be operated using a method according to an embodiment of the invention, but which is only for illustration purposes with a significantly higher one
  • Plate stack is shown. 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 used of the header 5 distributed over a group of heat exchanger plates 4 of the modules 1, 2. After the fluid fed in by means of the header 5 has flowed through the modules 1, 2, it is collected by means of the header 6 and, in the cooled state, is discharged via a connection piece (not visible here).
  • a cold fluid is distributed to another group of heat exchanger plates 4 of the modules 1, 2 by means of the header 7. After the fluid fed in by means of the header 7 has flowed through the modules 1, 2, it is collected by means of the header 8 and, in the heated state, is discharged via the nozzle 81.
  • a corresponding one is used of the header 5 distributed over a group of heat exchanger plates 4 of the modules 1, 2. After the fluid fed in by means of the header 5 has flowed through the modules 1, 2, it is collected by means of the
  • 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 designated here as 11 and a second end designated here as 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 first
  • second certain
  • a heat exchanger 100 which is constructed from a plurality of modules 1, 2 and is connected to one another by means of corresponding module connections 3.
  • 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.
  • FIG. 3 illustrates a relationship between fluid flows and thermal stresses in a fin-plate heat exchanger.
  • FIG. 3 shows a standardized cold mass flow in dimensionless units, that is to say an amount of cold fluid supplied to the heat exchanger per unit of time, on the
  • the abscissa and a normalized maximum thermal stress are plotted on the ordinate in dimensionless units.
  • 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.
  • a quantity of fluid is only increased when the areas in which module connections of a finned-plate heat exchanger constructed from a plurality of modules, for example a heat exchanger as shown in FIG. 2, are arranged are sufficiently temperature-controlled, since such Areas particularly negative effects of thermal stresses. This is further explained with reference to FIG. 4.
  • 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 of 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 i.e. from the transition from the second to the first operating mode, starting from the two ends as time progresses to the inside of the heat exchanger or the
  • Heat exchange zone set. If the heat exchanger, e.g. in a sensitive area of module connections, already experiencing the greatest temperature changes occurring during the transition to the first operating mode, only reduced gradients occur here, and thus greatly reduced
  • Heat exchanger for example the heat exchanger 100 shown in Figure 2 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 sub-zones are also denoted here in the diagram 410 by 10, 13 and 14.
  • the time illustrated with diagram 410 there was only a slight change in temperature at the extreme ends of the
  • Heat exchange zone 10 result, which initially only affects the sub-zones 13 and 14. Temperature profiles 402 to 406 arise with increasing time. The highest voltages occur in particular when the one that arises
  • Temperature gradient is present at the inner end of the module connections here, which is approximately the case at the times indicated here with the diagrams 430 and 440.
  • corresponding thermal voltages are reduced, in particular, by deliberately lowering those periods in which the areas of the module connections experience large temperature changes
  • FIG. 5 schematically illustrates a plant for nitrogen liquefaction, which can be operated using a method according to an embodiment of the invention, and is designated overall by 500.
  • the system 500 illustrated in FIG. 1 has in particular one
  • Heat exchanger on. 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. Part of the compressed gaseous nitrogen (stream b) is in
  • Turbine boosters 520, 530 which are each provided with aftercoolers, further compressed 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, in an expansion turbine
  • Turbine boosters 520 relaxed 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 together with gaseous nitrogen from the container 540 as stream f at one
  • 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 carried in the stream k
  • gaseous nitrogen is fed via stream I to stream a and thus back 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)

Abstract

La présente invention concerne un procédé destiné à faire fonctionner un échangeur de chaleur (100) qui comporte une zone d'échange (10) de chaleur qui s'étend entre une première extrémité (11) et une deuxième extrémité (12) et qui comporte un empilement de plaques en plaques (4) d'échangeur de chaleur, une largeur des plaques (4) d'échangeur de chaleur et une hauteur de l'empilement de plaques étant comprises entre un tiers et un cinquième d'une longueur des plaques (4) d'échangeur de chaleur entre la première extrémité (11) et la deuxième extrémité (11). Après la mise à l'arrêt et après qu'un état d'équilibre de température est atteint, des fluides qui sont conduits respectivement en fonctionnement normal dans une première quantité par unité de temps à travers la zone d'échange (10) de chaleur, sont conduits lors d'une remise en fonctionnement jusqu'à un instant d'élévation d'abord respectivement dans une deuxième quantité par unité de temps qui est inférieure à la première quantité par unité de temps à travers la première zone d'échange (10) et à partir de l'instant d'élévation respectivement dans la première quantité par unité de temps à travers la première zone d'échange (10) de chaleur. L'invention a également pour objet un système correspondant qui est en particulier réalisé sous forme d'installation de traitement d'air.
PCT/EP2019/025222 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 WO2020011396A1 (fr)

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EP18020329.1 2018-07-13
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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FR3121504B1 (fr) * 2021-04-01 2023-04-14 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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US20020017468A1 (en) 2000-07-18 2002-02-14 Clay Forrest Kelly Apparatus and methods for packaging and distributing combinations of multi-pack beverage cartons and complementary containers
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DE102009042994A1 (de) 2009-09-25 2011-03-31 Linde Aktiengesellschaft Verfahren und Vorrichtung zur sicherheitstechnischen Überwachung eines thermisch belasteten Apparates
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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JP2004019987A (ja) * 2002-06-13 2004-01-22 Hitachi Ltd 深冷空気分離装置
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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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