EP0048316B1 - Process and installation for the revaporization of liquefied natural gas - Google Patents

Process and installation for the revaporization of liquefied natural gas Download PDF

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Publication number
EP0048316B1
EP0048316B1 EP19810104348 EP81104348A EP0048316B1 EP 0048316 B1 EP0048316 B1 EP 0048316B1 EP 19810104348 EP19810104348 EP 19810104348 EP 81104348 A EP81104348 A EP 81104348A EP 0048316 B1 EP0048316 B1 EP 0048316B1
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EP
European Patent Office
Prior art keywords
natural gas
circuit
evaporator
transfer medium
heat
Prior art date
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Expired
Application number
EP19810104348
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German (de)
French (fr)
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EP0048316A1 (en
Inventor
Lothar Ing.-Grad. Bauer
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ThyssenKrupp Industrial Solutions AG
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Uhde GmbH
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Classifications

    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C9/00—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure
    • F17C9/02—Methods or apparatus for discharging liquefied or solidified gases from vessels not under pressure with change of state, e.g. vaporisation
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2221/00—Handled fluid, in particular type of fluid
    • F17C2221/03—Mixtures
    • F17C2221/032—Hydrocarbons
    • F17C2221/033—Methane, e.g. natural gas, CNG, LNG, GNL, GNC, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/01—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the phase
    • F17C2223/0146—Two-phase
    • F17C2223/0153—Liquefied gas, e.g. LPG, GPL
    • F17C2223/0161—Liquefied gas, e.g. LPG, GPL cryogenic, e.g. LNG, GNL, PLNG
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/035—High pressure (>10 bar)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2223/00—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel
    • F17C2223/03—Handled fluid before transfer, i.e. state of fluid when stored in the vessel or before transfer from the vessel characterised by the pressure level
    • F17C2223/036—Very high pressure (>80 bar)
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F17C2227/0316—Water heating
    • F17C2227/0318—Water heating using seawater
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2227/00—Transfer of fluids, i.e. method or means for transferring the fluid; Heat exchange with the fluid
    • F17C2227/03—Heat exchange with the fluid
    • F17C2227/0367—Localisation of heat exchange
    • F17C2227/0388—Localisation of heat exchange separate
    • F17C2227/0393—Localisation of heat exchange separate using a vaporiser
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F17—STORING OR DISTRIBUTING GASES OR LIQUIDS
    • F17C—VESSELS FOR CONTAINING OR STORING COMPRESSED, LIQUEFIED OR SOLIDIFIED GASES; FIXED-CAPACITY GAS-HOLDERS; FILLING VESSELS WITH, OR DISCHARGING FROM VESSELS, COMPRESSED, LIQUEFIED, OR SOLIDIFIED GASES
    • F17C2250/00—Accessories; Control means; Indicating, measuring or monitoring of parameters
    • F17C2250/06—Controlling or regulating of parameters as output values
    • F17C2250/0605—Parameters
    • F17C2250/0636—Flow or movement of content

Definitions

  • the invention relates to a process for the re-evaporation of liquid natural gas, using a heat transfer medium which is conducted in a closed circuit containing a heat dispenser, in particular a seawater-charged heat exchanger and a natural gas evaporator, and a second circulating circuit with a further energy supply, and to a plant to carry out this process.
  • a heat dispenser in particular a seawater-charged heat exchanger and a natural gas evaporator
  • a second circulating circuit with a further energy supply
  • a heat transfer medium is condensed in two pressure stages, a main stream evaporating in an evaporator exposed to sea water and condensed with heat being given off to a heat exchanger through which natural gas flows, and a secondary stream of the heat transfer medium branching off from this main stream from one Pressure increasing device brought to a higher pressure level and releases its energy in a natural gas superheater and then brought back to the pressure of the main stream in a pressure reducing device and supplied to it.
  • the known method has the particular disadvantage that it cannot be adapted to the respective site conditions of such a system to the desired extent and, in particular, can react very clumsily to different temperatures of the evaporator exposed to sea water.
  • pressure booster and pressure reduction systems consume energy that is lost in the overall process.
  • This object is achieved in a method of the type described in the introduction in that the heat transfer medium in the first partial circuit between the sea water heat exchanger and the natural gas evaporator is circulated in the natural cycle and in the second partial circuit as a liquid phase another heat exchanger as a secondary heat source and the natural gas evaporator in the first partial circuit the same pressure is supplied in the natural gas evaporator, the partial quantity being regulated via the seawater inlet temperature.
  • the overall process without external heat supply i.e. H. be operated exclusively with sea water if its inlet temperature is correspondingly high.
  • the sea water temperature drops in winter, additional energy can be supplied via a partial flow, the partial flow circuits generally being able to be maintained over very wide areas in natural circulation. This means that the external energy can be adapted to the individual environmental conditions.
  • the invention provides that the natural gas evaporator is followed by a natural gas superheater, which is supplied with additional energy by a further, independent heat transfer medium circuit, and in particular it can also be provided that the heat transfer medium circuit of the natural gas superheater is operated at a higher pressure level than that in the natural gas evaporator .
  • the energy supply to the second sub-circuit and / or to the additional circuit of the heat transfer medium takes place via a secondary heat source, it being possible for the liquid natural gas to be evaporated in one or two stages from the heat transfer medium in tube bundle heat exchangers, where In a further embodiment it can be provided that an immersion flame evaporator and / or the exhaust gas from a power plant is used as the secondary heat source.
  • the invention also provides a system for carrying out the above-described method, which is characterized in particular by at least one heat exchanger acted upon by sea water as an evaporator of the heat transfer medium and a heat exchanger arranged in its circuit as a natural gas evaporator and a heat exchanger medium collector associated with or downstream of the natural gas evaporator distinguishes first partial circuit and a second partial circuit and a regulation for regulating the partial amount in the second partial circuit via the seawater inlet temperature.
  • This inventive design of the system has the advantage that large amounts of sea water can be used, as well as the Ge total volume of the partial flows of the heat transfer medium can be kept very large, so that an overall very large plant performance can be achieved.
  • a wide range of sea water temperatures can be driven without the need for an external energy supply if the sea water has a correspondingly high inlet temperature into the system.
  • a further heat exchanger is connected downstream as a natural gas superheater in the direction of the natural gas flow, the heat exchanger and the collector of the heat transfer medium being connected together with the further heat supply devices in the circuits.
  • immersion flame evaporators are provided as further heat supply devices for the heat transfer medium and these are heated with natural gas, or that the immersion flame evaporators are externally heated or circulated via an exhaust gas cooler of a thermal power plant, which can also be provided according to the invention .
  • To control the entire system is a control that switches on the heat transfer medium circuit via the secondary heat source when the permissible sea water temperature drops, the partial circuit being conducted via the hot water of the submersible flame evaporator heated by power plant waste heat and switching on a burner of the submersible flame evaporator or additional additional heat transfer medium circuit for additional energy requirements Switches on the superheater.
  • a heat transfer medium preferably propane (hereinafter only the heat transfer medium is referred to as propane) is conducted in a first sub-circuit I between a propane evaporator 1 exposed to sea water and a natural gas evaporator 2.
  • propane a heat transfer medium
  • the sea water enters the propane evaporator 1 at 3 and leaves it at 4.
  • the natural gas enters the natural gas evaporator at 5 and leaves it via line 6.
  • the natural gas which is initially still liquid in the propane evaporator 1 is evaporated by the sea water and exits via a line 7 from the gas dome 8 of the propane evaporator 1 and into the natural gas evaporator 2 at the top.
  • the propane condenses with heat being given off at the evaporator coils of the natural gas evaporator 2 and is deposited as liquid propane in the sump 9 of the natural gas evaporator 2, from where it is fed back to the propane evaporator 1 in liquid form via a line 10, closing the circuit.
  • a further propane circuit 11 is provided in parallel to the former.
  • a partial flow of the propane is withdrawn from the propane evaporator 1 via a line 11 and, if necessary, via a pump 12, in particular to overcome the pipeline losses, to a heat source, for.
  • B. a submersible flame evaporator 13, passed there and evaporated via a line 14 to the natural gas evaporator 2, condensed there and given as condensate via line 10 again closing the circuit 11 to the propane evaporator 1.
  • the circuits I and 11 can be operated in natural circulation, should large pipe friction losses or other system losses occur, both circuits can, however, be operated in the forced circulation at the same pressure level.
  • a natural gas superheater 15 is shown with a natural gas line 16, which is also acted upon by propane.
  • This further propane circuit is designated 111 and leads from the natural gas superheater 15 via a line 17, possibly via a pump 18 to a further heat source, e.g. B. a submersible flame evaporator 19, and a line 20 back to the natural gas superheater.
  • the heat source 19 and the heat source 13 can be identical or can be provided within the same component.
  • both the heat exchanger coils of the heat source 19 and that of the heat source 13 can be arranged within the same basin.
  • the higher energy level required for overheating is achieved in that the circuit 111 is operated at a higher total pressure than the circuits and 11.
  • FIG. 2 a modified process control is shown as a schematic diagram compared to the arrangement of FIG. 1.
  • the refrigerant circuit I in FIG. 1 corresponds to two propane circuits "A" and "A '", the propane being conducted via seawater-heated propane evaporators 21 and 21' and a natural gas evaporator 22 and a propane collector 23.
  • the circuit lines of the circuits "A" and "A '" are not specified.
  • the seawater inlet and outlet is designated 3 'or 4' in accordance with FIG. 1, just as the inlet of the liquid natural gas is designated 5 'and the outlet of the gaseous superheated natural gas is designated 6' or 16 'in accordance with FIG. 1.
  • the The partial quantity circuit 11 corresponding to FIG. 1 is designated by “B” in FIG. 2.
  • the propane is supplied to the natural gas evaporator 22 via a line 11 ', a pump 12' and a submerged flame evaporator 13 'and via a line 14'.
  • the additional propane circuit 111 according to FIG. 1 is designated by “C” in FIG. It leads from the immersion flame evaporator 13 'via a line 24 to a natural gas superheater 25 and via the natural gas evaporator 22, the propane collector 23, the line 11', the pump 12 'back to the immersion flame evaporator 13'.
  • the water of the submerged flame evaporator 13 ′ can be passed through a further circuit labeled “D” and, if appropriate, preheated in a waste gas cooler 27 by exhaust gas from a power plant, the inlet of which is labeled 26.
  • the burner 28 of the immersion flame evaporator 13 ' can be acted upon by natural gas via the line 29.
  • the water supply to the submerged flame evaporator 13 ' is designated 30.
  • the system is regulated in connection with FIG. 1 as follows: depending on the water temperature at the seawater inlet 3, the additional heat supply via the circuit 11 at the heat source 13 is regulated by means of appropriate regulators.
  • the subset of the circuit 11 can be driven from 0-100%, i. H. the circuit 11 can be switched off (0%) or the entire amount of propane, including that of the circuit I; Promote via the secondary heat source (100%).
  • the discharge temperature of the gasified natural gas is measured at 6 and, if necessary, the additional circuit 111 is switched on in order to obtain the required natural gas temperature at 16.
  • This regulation is basically the same in the exemplary embodiment according to FIG. 2, where larger quantities can be implemented by connecting at least two seawater-heated propane evaporators in parallel. In the event of a device failure or icing, appropriate measures can be taken to return heated propane through these evaporators and thus de-icing. Depending on the occurrence of power plant exhaust gases in the circuit "D", the burner 28 can be switched off completely or can be operated with a slight excess.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)

Description

Die Erfindung richtet sich auf ein Verfahren zur Rückverdampfung von flüssigem Erdgas, unter Einsatz eines Wärmeübertragungsmediums, welches in einem geschlossenen, einen Wärmespender, insbesondere einen meerwasserbeaufschlagten Wärmetauscher und einen Erdgasverdampfer enthaltenden ersten Kreislauf und einem zweiten im Zwangsumlauf geführten Teilkreislauf mit einer weiteren Energiezufuhr geführt ist sowie auf eine Anlage zur Durchführung dieses Verfahrens.The invention relates to a process for the re-evaporation of liquid natural gas, using a heat transfer medium which is conducted in a closed circuit containing a heat dispenser, in particular a seawater-charged heat exchanger and a natural gas evaporator, and a second circulating circuit with a further energy supply, and to a plant to carry out this process.

Bei einem bekannten Verfahren (DE-B-2 751 642) wird ein Wärmeübertragungsmedium in zwei Druckstufen kondensiert, wobei ein Hauptstrom in einem meerwasserbeaufschlagten Verdampfer verdampft und unter Wärmeabgabe an einem vom Erdgas durchströmten Wärmetauscher kondensiert und ein von diesem Hauptstrom abzweigender Nebenstrom des Wärmeübertragungsmediums von einer Druckerhöhungseinrichtung auf ein höheres Druckniveau gebracht und seine Energie in einem Erdgasüberhitzer abgibt und anschließend in einer Druckminderungseinrichtung wieder auf den Druck des Hauptstromes gebracht und diesem zugeführt wird. Das bekannte Verfahren hat insbesondere den Nachteil, daß es nicht im gewünschten Maße den jeweiligen Standortbedingungen einer solchen Anlage anpaßbar ist und insbesondere sehr schwerfällig auf unterschiedliche Temperaturen des meerwasserbeaufschlagten Verdampfers reagieren kann. Darüber hinaus verbrauchen Druckerhöhungs- und Druckniedrigungsanlagen Energie, die dem Gesamtprozeß verlorengeht.In a known method (DE-B-2 751 642), a heat transfer medium is condensed in two pressure stages, a main stream evaporating in an evaporator exposed to sea water and condensed with heat being given off to a heat exchanger through which natural gas flows, and a secondary stream of the heat transfer medium branching off from this main stream from one Pressure increasing device brought to a higher pressure level and releases its energy in a natural gas superheater and then brought back to the pressure of the main stream in a pressure reducing device and supplied to it. The known method has the particular disadvantage that it cannot be adapted to the respective site conditions of such a system to the desired extent and, in particular, can react very clumsily to different temperatures of the evaporator exposed to sea water. In addition, pressure booster and pressure reduction systems consume energy that is lost in the overall process.

Demgegenüber ist es Aufgabe der Erfindung, ein Verfahren sowie eine Anlage zur Durchführung eines eingangs bezeichneten Verfahrens anzugeben, bei dem eine Anpassung an Meerwassertemperaturschwankungen in einfacher Weise möglich und die Zufuhr von Fremdenergie auf ein Mindestmaß reduzierbar ist.In contrast, it is an object of the invention to provide a method and a system for carrying out a method described in the introduction, in which an adaptation to sea water temperature fluctuations is possible in a simple manner and the supply of external energy can be reduced to a minimum.

Diese Aufgabe wird bei einem Verfahren der eingangs bezeichneten Art dadurch gelöst, daß das Wärmeübertragungsmedium im ersten Teilkreislauf zwischen dem Meerwasser-Wärmetauscher und dem Erdgasverdampfer im Naturumlauf geführt wird und im zweiten Teilkreislauf als flüssige Phase einem weiteren Wärmetauscher als Sekundärwärmequelle und dem Erdgasverdampfer bei zum ersten Teilkreislauf gleichem Druck im Erdgasverdampfer zugeführt wird, wobei eine Regelung der Teilmenge über die Meerwassereintrittstemperatur erfolgt.This object is achieved in a method of the type described in the introduction in that the heat transfer medium in the first partial circuit between the sea water heat exchanger and the natural gas evaporator is circulated in the natural cycle and in the second partial circuit as a liquid phase another heat exchanger as a secondary heat source and the natural gas evaporator in the first partial circuit the same pressure is supplied in the natural gas evaporator, the partial quantity being regulated via the seawater inlet temperature.

Durch das Vorsehen von Teilkreisläufen, bereits im Bereich des Erdgasverdampfers, mit neben der Möglichkeit der bekannten Wärmezufuhr durch Meerwasser gesonderter Wärmezufuhr in einem Teilkreislauf und die Regelung über die Meerwassereintrittstemperatur kann je nach Außenbedingungen der Gesamtprozeß ohne externe Wärmezufuhr, d. h. ausschließlich mit Meerwasser betrieben werden, wenn dessen Eintrittstemperatur entsprechend hoch ist. Wenn beispielsweise jedoch im Winter die Meerwassertemperatur absinkt, kann über einen Teilstrom zusätzliche Energie zugeführt werden, wobei die Teilstromkreisläufe in der Regel über sehr weite Bereiche im Naturumlauf aufrechterhalten werden können. Dies bedeutet, daß die Fremdenergie jeweils den individuellen Umgebungsbedingungen angepaßt werden kann.By providing partial circuits, already in the area of the natural gas evaporator, in addition to the possibility of the known heat supply by sea water, separate heat supply in a partial circuit and the regulation via the sea water inlet temperature, depending on the external conditions, the overall process without external heat supply, i.e. H. be operated exclusively with sea water if its inlet temperature is correspondingly high. However, if, for example, the sea water temperature drops in winter, additional energy can be supplied via a partial flow, the partial flow circuits generally being able to be maintained over very wide areas in natural circulation. This means that the external energy can be adapted to the individual environmental conditions.

In Ausgestaltung sieht die Erfindung vor, daß dem Erdgasverdampfer ein Erdgasüberhitzer nachgeschaltet wird, der von einem weiteren, unabhängigen Wärmeübertragungsmediumkreislauf mit zusätzlicher Energiezufuhr beaufschlagt wird, wobei insbesondere auch vorgesehen sein kann, daß der Wärmeübertragungsmediumkreislauf des Erdgasüberhitzers bei einem höheren Druckniveau betrieben wird als demjenigen im Erdgasverdampfer.In an embodiment, the invention provides that the natural gas evaporator is followed by a natural gas superheater, which is supplied with additional energy by a further, independent heat transfer medium circuit, and in particular it can also be provided that the heat transfer medium circuit of the natural gas superheater is operated at a higher pressure level than that in the natural gas evaporator .

Aus der eingangs erwähnten DE-A-2 751 642 ist das Vorsehen eines Überhitzers bekannt, der von einem Wärmeübertragungsmedium mit höherem Druck beaufschlagt ist. Wesentlich für die Erfindung ist im vorliegenden Fall, daß der Überhitzungskreislauf des Wärmeübertragungsmediums in sich geschlossen auf einem höheren Druckniveau betrieben wird, so daß in einem solchen Kreislauf Druckerhöhungs- bzw. Druckminderungsanlagen entbehrlich sind, die das Wärmeübertragungsmedium den Drücken der Teilkreisläufe der vorgeschalteten Prozesse anpassen müßten. Damit ist eine weitere, gegenüber der bekannten Verfahrensweise wirtschaftlichere Lösung des Prozeßablaufes gegeben.From the aforementioned DE-A-2 751 642 it is known to provide a superheater which is subjected to a higher pressure by a heat transfer medium. It is essential for the invention in the present case that the overheating circuit of the heat transfer medium is operated in a closed manner at a higher pressure level, so that in such a circuit pressure booster or pressure reduction systems are unnecessary, which would have to adapt the heat transfer medium to the pressures of the sub-circuits of the upstream processes . This provides a further, more economical solution to the process flow compared to the known procedure.

Nach der Erfindung kann auch vorgesehen sein, daß die Energiezufuhr zu dem zweiten Teilkreislauf und/oder zum zusätzlichen Kreislauf des Wärmeübertragungsmediums über eine Sekundärwärmequelle erfolgt, wobei es vorteilhaft sein kann, wenn das flüssige Erdgas in Rohrbündelwärmetauschern ein- oder zweistufig vom Wärmeübertragungsmedium verdampft wird, wobei in weiterer Ausgestaltung vorgesehen sein kann, daß als Sekundärwärmequelle ein Tauchflammenverdampfer und/oder das Abgas aus einem Kraftwerk eingesetzt wird.According to the invention it can also be provided that the energy supply to the second sub-circuit and / or to the additional circuit of the heat transfer medium takes place via a secondary heat source, it being possible for the liquid natural gas to be evaporated in one or two stages from the heat transfer medium in tube bundle heat exchangers, where In a further embodiment it can be provided that an immersion flame evaporator and / or the exhaust gas from a power plant is used as the secondary heat source.

Die Erfindung sieht auch eine Anlage zur Durchführung des vorbeschriebenen Verfahrens vor, welches sich insbesondere durch wenigstens einen vom Meerwasser beaufschlagten Wärmetauscher als Verdampfer des Wärmeübertragungsmediums sowie einen in dessen Kreislauf angeordneten Wärmetauscher als Erdgasverdampfer und einen dem Erdgasverdampfer zu- bzw. nachgeordneten Wärmetauschermedium-Sammler mit einem ersten Teilkreislauf und einem zweiten Teilkreislauf und einer Regelung zur Regelung der Teilmenge im zweiten Teilkreislauf über die Meerwassereintrittstemperatur auszeichnet.The invention also provides a system for carrying out the above-described method, which is characterized in particular by at least one heat exchanger acted upon by sea water as an evaporator of the heat transfer medium and a heat exchanger arranged in its circuit as a natural gas evaporator and a heat exchanger medium collector associated with or downstream of the natural gas evaporator distinguishes first partial circuit and a second partial circuit and a regulation for regulating the partial amount in the second partial circuit via the seawater inlet temperature.

Diese erfindungsgemäße Ausgestaltung der Anlage hat den Vorteil, daß große Mengen Meerwasser einsetzbar sind, ebenso wie das Gesamtvolumen der Teilströme des Wärmeübertragungsmediums sehr groß gehalten werden kann, so daß sich eine insgesamt sehr große Anlagenleistungen erreichen läßt. Gleichzeitig kann durch entsprechende Steuerung des Natur- bzw. Zwangsumlaufes bei der gewählten Anordnung ein breiter Bereich von Meerwassertemperaturen gefahren werden, ohne daß es einer externen Energiezufuhr bedarf, wenn das Meerwasser eine entsprechend hohe Eintrittstemperatur in die Anlage aufweist. Es ist auch möglich, z. B. bei Frostgefahr, einen Wärmetauscher wärme- übertragungsmediumseitig abzuschalten, wobei das Meerwasser weiterströmt. Dadurch wird das Wärmeübertragungsmedium in den Sammler verlagert und der Wärmetauscher entsprechend vom Meerwasser erwärmt.This inventive design of the system has the advantage that large amounts of sea water can be used, as well as the Ge total volume of the partial flows of the heat transfer medium can be kept very large, so that an overall very large plant performance can be achieved. At the same time, by appropriately controlling the natural or forced circulation in the selected arrangement, a wide range of sea water temperatures can be driven without the need for an external energy supply if the sea water has a correspondingly high inlet temperature into the system. It is also possible e.g. B. if there is a risk of frost, switching off a heat exchanger on the heat transfer medium side, with the sea water continuing to flow. As a result, the heat transfer medium is transferred to the collector and the heat exchanger is heated accordingly by the sea water.

In Ausgestaltung ist nach der Erfindung vorgesehen, daß in Richtung des Erdgasdurchflusses einem ersten Wärmetauscher ein weiterer Wärmetauscher als Erdgasüberhitzer nachgeschaltet ist, wobei die Wärmetauscher sowie der Sammler des Wärmeübertragungsmediums mit den weiteren Wärmezuführeinrichtungen in den Kreisläufen zusammengeschaltet sind.In an embodiment it is provided according to the invention that a further heat exchanger is connected downstream as a natural gas superheater in the direction of the natural gas flow, the heat exchanger and the collector of the heat transfer medium being connected together with the further heat supply devices in the circuits.

Nach der Erfindung kann auch vorgesehen sein, daß als weitere Wärmezuführeinrichtungen für das Wärmeübertragungsmedium Tauchflammenverdampfer vorgesehen und diese mit Erdgas beheizt sind, oder aber daß die Tauchflammenverdampfer fremdbeheizt bzw. im Kreislauf über einen Abgaskühler eines Wärmekraftwerkes geführt sind, was nach der Erfindung auch vorgesehen sein kann.According to the invention it can also be provided that immersion flame evaporators are provided as further heat supply devices for the heat transfer medium and these are heated with natural gas, or that the immersion flame evaporators are externally heated or circulated via an exhaust gas cooler of a thermal power plant, which can also be provided according to the invention .

Zur Steuerung der Gesamtanlage ist eine Regelung, die bei Absinken der zulässigen Seewassertemperatur den Wärmeübertragungsmittelkreislauf über die Sekundärwärmequelle zuschaltet, wobei der Teilkreislauf über das von einer Kraftwerksabwärme beheizte Warmwasser des Tauchflammenverdampfers geführt und bei zusätzlichem Energiebedarf einen Brenner des Tauchflammenverdampfers zuschaltet bzw. den weiteren zusätzlichen Wärmeübertragungsmittelkreislauf zum Überhitzer einschaltet.To control the entire system is a control that switches on the heat transfer medium circuit via the secondary heat source when the permissible sea water temperature drops, the partial circuit being conducted via the hot water of the submersible flame evaporator heated by power plant waste heat and switching on a burner of the submersible flame evaporator or additional additional heat transfer medium circuit for additional energy requirements Switches on the superheater.

Die Erfindung ist nachstehend anhand der Zeichnung beispielsweise näher erläutert. Diese zeigt in

  • Fig. 1 ein Prinzipschaltbild des erfindungsgemäßen Verfahrens sowie in
  • Fig. 2 ein Prinzipschaltbild einer Anlage zur Durchführung des Verfahrens nach der Erfindung in einem bevorzugten Ausführungsbeispiel.
The invention is explained below with reference to the drawing, for example. This shows in
  • Fig. 1 is a schematic diagram of the method according to the invention and in
  • Fig. 2 is a schematic diagram of a system for performing the method according to the invention in a preferred embodiment.

Nach dem in Fig. 1 dargestellten Prinzipschaltbild wird ein Wärmeübertragungsmedium, vorzugsweise Propan (im folgenden wird ausschließlich das Wärmeübertragungsmedium als Propan bezeichnet) in einem ersten Teilkreislauf I zwischen einem meerwasserbeaufschlagten Propan-Verdampfer 1 und einen Erdgasverdampfer 2 geführt. Das Meerwasser tritt bei 3 in den Propan-Verdampfer 1 ein und verläßt diesen bei 4. Das Erdgas tritt in den Erdgasverdampfer bei 5 ein und verläßt ihn über die Leitung 6. Das im Propan-Verdampfer 1 zunächst noch flüssige Erdgas wird durch das Meerwasser verdampft und tritt über eine Leitung 7 aus dem Gasdom 8 des Propan-Verdampfers 1 aus und in den Erdgasverdampfer 2 oben ein. Dort kondensiert das Propan unter Wärmeabgabe an den Verdampferschlangen des Erdgasverdampfers 2 und schlägt sich als flüssiges Propan im Sumpf 9 des Erdgasverdampfers 2 nieder, von wo es über eine Leitung 10 flüssig dem Propan-Verdampfer 1 unter Schließung des Kreises wieder zugeführt wird.According to the basic circuit diagram shown in FIG. 1, a heat transfer medium, preferably propane (hereinafter only the heat transfer medium is referred to as propane) is conducted in a first sub-circuit I between a propane evaporator 1 exposed to sea water and a natural gas evaporator 2. The sea water enters the propane evaporator 1 at 3 and leaves it at 4. The natural gas enters the natural gas evaporator at 5 and leaves it via line 6. The natural gas which is initially still liquid in the propane evaporator 1 is evaporated by the sea water and exits via a line 7 from the gas dome 8 of the propane evaporator 1 and into the natural gas evaporator 2 at the top. There, the propane condenses with heat being given off at the evaporator coils of the natural gas evaporator 2 and is deposited as liquid propane in the sump 9 of the natural gas evaporator 2, from where it is fed back to the propane evaporator 1 in liquid form via a line 10, closing the circuit.

Neben dem Propankreislauf ist ein weiterer Propankreislauf 11 parallel zum ersteren vorgesehen. Ein Teilstrom des Propans wird über eine Leitung 11 dem Propan-Verdampfer 1 entzogen und ggf. über eine Pumpe 12, insbesondere zur Überwindung der Rohrleitungsverluste, weiter zu einer Wärmequelle, z. B. einem Tauchflammenverdampfer 13, geführt, dort verdampft und über eine Leitung 14 dem Erdgasverdampfer 2 zugeführt, dort kondensiert und als Kondensat über die Leitung 10 unter Schließung des Kreises 11 erneut dem Propan-Verdampfer 1 aufgegeben.In addition to the propane circuit, a further propane circuit 11 is provided in parallel to the former. A partial flow of the propane is withdrawn from the propane evaporator 1 via a line 11 and, if necessary, via a pump 12, in particular to overcome the pipeline losses, to a heat source, for. B. a submersible flame evaporator 13, passed there and evaporated via a line 14 to the natural gas evaporator 2, condensed there and given as condensate via line 10 again closing the circuit 11 to the propane evaporator 1.

Die Kreisläufe I und 11 können im Naturumlauf gefahren werden, sollten große Rohrreibungsverluste oder sonstige Systemverluste auftreten, können beide Kreisläufe im Zwangsumlauf jedoch auf gleichem Druckniveau geführt werden.The circuits I and 11 can be operated in natural circulation, should large pipe friction losses or other system losses occur, both circuits can, however, be operated in the forced circulation at the same pressure level.

In Fig. 1 ist noch ein Erdgasüberhitzer 15 mit einer Erdgasleitung 16 dargestellt, der ebenfalls von Propan beaufschlagt ist. Dieser weitere Propankreislauf ist mit 111 bezeichnet und führt von dem Erdgasüberhitzer 15 über eine Leitung 17, ggf. über eine Pumpe 18 zu einer weiteren Wärmequelle, z. B. einem Tauchflammenverdampfer 19, und eine Leitung 20 zurück zum Erdgasüberhitzer. Die Wärmequelle 19 und die Wärmequelle 13 können identisch bzw. innerhalb eines gleichen Bauteils vorgesehen sein. So können sowohl die Wärmetauscherschlangen der Wärmequelle 19 als auch die der Wärmequelle 13 innerhalb eines gleichen Beckens angeordnet sein. Das zur Überhitzung erforderliche höhere Energieniveau wird dadurch erreicht, daß der Kreislauf 111 bei einem höheren Gesamtdruck betrieben wird als die Kreisläufe und 11.In Fig. 1, a natural gas superheater 15 is shown with a natural gas line 16, which is also acted upon by propane. This further propane circuit is designated 111 and leads from the natural gas superheater 15 via a line 17, possibly via a pump 18 to a further heat source, e.g. B. a submersible flame evaporator 19, and a line 20 back to the natural gas superheater. The heat source 19 and the heat source 13 can be identical or can be provided within the same component. Thus, both the heat exchanger coils of the heat source 19 and that of the heat source 13 can be arranged within the same basin. The higher energy level required for overheating is achieved in that the circuit 111 is operated at a higher total pressure than the circuits and 11.

In Fig. 2 ist gegenüber der Anordnung nach Fig. 1 eine modifizierte Prozeßführung als Prinzipskizze dargestellt. Zur besseren Identifizierung der unterschiedlichen Kältemittel-Kreisläufe sind in Fig. 2 zur Bezeichnung der Kreisläufe Großbuchstaben herangezogen. So entspricht dem Kältemittel-Kreislauf I in Fig. 1 zwei Propankreisläufen »A« und »A'«, wobei das Propan über meerwasserbeheizte Propan-Verdampfer 21 und 21' und einen Erdgasverdampfer 22 sowie einen Propansammler 23 geführt ist.In Fig. 2 a modified process control is shown as a schematic diagram compared to the arrangement of FIG. 1. To better identify the different refrigerant circuits, capital letters are used in FIG. 2 to designate the circuits. The refrigerant circuit I in FIG. 1 corresponds to two propane circuits "A" and "A '", the propane being conducted via seawater-heated propane evaporators 21 and 21' and a natural gas evaporator 22 and a propane collector 23.

Die Kreislaufleitungen der Kreisläufe »A« und »A'« sind nicht näher bezeichnet. Der Meerwassereintritt und -austritt ist entsprechend Fig. 1 mit 3' bzw. 4' bezeichnet, ebenso wie der Eintritt des flüssigen Erdgases mit 5' und der Austritt des gasförmigen überhitzten Erdgases entsprechend Fig. 1 mit 6' bzw. 16' bezeichnet ist. Der der Fig. 1 entsprechende Teilmengenkreislauf 11 ist in Fig. 2 mit »B« bezeichnet. Das Propan wird bei diesem Kreislauf über eine Leitung 11', eine Pumpe 12' und einen Tauchflammenverdampfer 13' sowie über eine Leitung 14' dem Erdgasverdampfer 22 zugeführt.The circuit lines of the circuits "A" and "A '" are not specified. The seawater inlet and outlet is designated 3 'or 4' in accordance with FIG. 1, just as the inlet of the liquid natural gas is designated 5 'and the outlet of the gaseous superheated natural gas is designated 6' or 16 'in accordance with FIG. 1. The The partial quantity circuit 11 corresponding to FIG. 1 is designated by “B” in FIG. 2. In this circuit, the propane is supplied to the natural gas evaporator 22 via a line 11 ', a pump 12' and a submerged flame evaporator 13 'and via a line 14'.

Der zusätzliche Propankreislauf 111 nach Fig. 1 ist in Fig.2 mit »C« bezeichnet. Er führt vom Tauchflammenverdampfer 13' über eine Leitung 24 zu einem Erdgasüberhitzer 25 und über den Erdgasverdampfer 22, dem Propansammler 23, die Leitung 11', die Pumpe 12'zurück zum Tauchflammenverdampfer 13'.The additional propane circuit 111 according to FIG. 1 is designated by “C” in FIG. It leads from the immersion flame evaporator 13 'via a line 24 to a natural gas superheater 25 and via the natural gas evaporator 22, the propane collector 23, the line 11', the pump 12 'back to the immersion flame evaporator 13'.

Das Wasser des Tauchflammenverdampfers 13' kann über einen weiteren mit »D« bezeichneten Kreislauf geführt und ggf. von Abgas aus einem Kraftwerk, dessen Eintritt mit 26 bezeichnet ist, in einem Abgaskühler 27 vorgewärmt sein. Der Brenner 28 des Tauchflammenverdampfers 13' kann von Erdgas über die Leitung 29 beaufschlagt sein. Die Wasserzufuhr zum Tauchflammenverdampfer 13' ist mit 30 bezeichnet.The water of the submerged flame evaporator 13 ′ can be passed through a further circuit labeled “D” and, if appropriate, preheated in a waste gas cooler 27 by exhaust gas from a power plant, the inlet of which is labeled 26. The burner 28 of the immersion flame evaporator 13 'can be acted upon by natural gas via the line 29. The water supply to the submerged flame evaporator 13 'is designated 30.

Die Regelung der Anlage erfolgt dabei in Verbindung mit Fig. 1 wie folgt: Je nach Wassertemperatur am Meerwassereinlauf 3 wird über entsprechende Regler die zusätzliche Wärmezufuhr über den Kreislauf 11 bei der Wärmequelle 13 geregelt. Die Teilmenge des Kreislaufes 11 kann von 0-100% gefahren werden, d. h. der Kreislauf 11 kann abgeschaltet sein (0%) oder die gesamte Propanmenge, auch die des Kreislaufes I; über die Sekundärwärmequelle fördern (100%). Dabei wird zusätzlich die Abgabetemperatur des vergasten Erdgases bei 6 gemessen und ggf. der zusätzliche Kreislauf 111 zugeschaltet, um bei 16 die erforderliche Erdgastemperatur zu erhalten.The system is regulated in connection with FIG. 1 as follows: depending on the water temperature at the seawater inlet 3, the additional heat supply via the circuit 11 at the heat source 13 is regulated by means of appropriate regulators. The subset of the circuit 11 can be driven from 0-100%, i. H. the circuit 11 can be switched off (0%) or the entire amount of propane, including that of the circuit I; Promote via the secondary heat source (100%). In addition, the discharge temperature of the gasified natural gas is measured at 6 and, if necessary, the additional circuit 111 is switched on in order to obtain the required natural gas temperature at 16.

Diese Regelung ist grundsätzlich beim Ausführungsbeispiel nach Fig. 2 die gleiche, dort können durch die Parallelschaltung von mindestens zwei meerwasserbeheizten Propan-Verdampfern größere Mengen umgesetzt werden. Auch kann bei Ausfall eines Gerätes oder bei Vereisung durch entsprechende Maßnahmen ein Rückfluß von erwärmten Propan durch diese Verdampfer und damit die Enteisung erreicht werden. Je nach Anfall von Kraftwerk-Abgasen im Kreislauf »D« kann der Brenner 28 vollständig abgeschaltet sein oder aber mit geringfügigem Überschuß gefahren werden.This regulation is basically the same in the exemplary embodiment according to FIG. 2, where larger quantities can be implemented by connecting at least two seawater-heated propane evaporators in parallel. In the event of a device failure or icing, appropriate measures can be taken to return heated propane through these evaporators and thus de-icing. Depending on the occurrence of power plant exhaust gases in the circuit "D", the burner 28 can be switched off completely or can be operated with a slight excess.

Neben den paarweise gefahrenen meerwasserbeaufschlagten Propan-Verdampfern können noch weitere Verdampfer ebenso wie weitere Überhitzer für das Erdgas in vergleichsweiser Schaltung vorgesehen sein. Auch ist die Erfindung nicht auf eine bestimmte zusätzliche Sekundärenergiequelle beschränkt. Hier können je nach Standort die ortsüblichen Zusatzenergiequellen herangezogen werden.In addition to the propane evaporators that are operated in pairs in sea water, further evaporators as well as further superheaters for the natural gas can be provided in a comparative circuit. The invention is also not restricted to a specific additional secondary energy source. Depending on the location, the local additional energy sources can be used here.

Claims (11)

1. A process for re-evaporating liqiud natural gas using a heat transfer medium which is circulated in a closed first circuit including a heat donor, in particular a sea water-fed heat exchanger, and a natural gas evaporator, and a second forced-circulation component circuit with a further supply of energy, characterised in that the heat transfer medium is circulated by natural circulation in the first component circuit between the sea water heat exchanger and the natural gas evaporator, and in the second component circuit is fed as a liquid phase to a further heat exchanger as a secondary heat source and to the natural gas evaporator at a pressure equal to the first component circuit in the natural gas evaporator, wherein regulation in respect of the partial amount involved is effected by way of the sea water inlet temperature.
2. A process according to claim 1 characterised in that disposed downstream of the natural gas evaporator is a natural gas superheater which receives an additional supply of energy from a further independent heat transfer medium circuit.
3. A process according to claim 2 characterised in that the heat transfer medium circuit of the natural gas superheater ist operated at a higher pressure level than that in the natural gas evaporator.
4. A process according to one of the preceding claims characterised in that the feed of energy to the second component circuit and/or to the additional circuit of the heat transfer medium is by way of a secondary heat source.
5. A process according to one of the preceding claims characterised in that the liquid natural gas is evaporated by the heat transfer medium in one or two stages in tube nest heat exchangers.
6. A process according to one of the preceding claims characterised in that the secondary heat source used is an immersion flame evaporator and/orthe exhaust gas from a power plant.
7. Installation for carrying out the process according to claim 1 for the re-evaporation of liquid natural gas using a circulated heat transfer medium chracterised by at least one heat exchanger (8 or 21) which is supplied with sea water as an evaporator for the heat transfer medium and a heat exchanger which is disposed in the circuit thereof (1, II or A) as a natural gas evaporator (2 or 22) and a heat exchange medium collector (9 or 23) associated with or disposed downstream of the natural gas evaporator, having a first component (I) and a second component circuit (II) and a regulating means for regulating the partial amount in the second component circuit (II) by way of the sea water inlet temperature.
8. Installation according to claim 7 characterised in that disposed downstream of a first heat exchanger (2 or 22), in the direction of the flow of natural gas, is a further heat exchanger as a natural gas superheater (15 or 25), wherein the heat exchanger (2, 15 or 22, 25) and the collector (23) are connected together with the further heat supply means (13) in the circuits (II, III or B, C).
9. Installation according to claim 8 characterised in that immersion flame evaporators (13) are provided as further heat supply means for the heat transfer medium, and said evaporators are heated with natural gas.
10. Installation according to claim 9 characterised in that the immersion flame evaporators (13) are separately heated or are disposed in the circuit (D) by way of an exhaust gas cooler (27) of a thermal power plant.
11. Installation according to claim 8, claim 9 or claim 10 characterised in that a regulating means which switches on the heat transfer medium circuit (II or B) by way of the secondary heat source (13) when the admissible sea water temperature falls, wherein the component circuit (II or B) is by way of the hot water, which is heated by a power plant waste heat, of the immersion flame evaporator (13) and, upon additional energy requirement, switches on a burner (28) of the flame evaporator (13) or switches on the further additional heat transfer medium circuit (III or C) to the superheater (15 or 25).
EP19810104348 1980-09-19 1981-06-05 Process and installation for the revaporization of liquefied natural gas Expired EP0048316B1 (en)

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DE3035349A DE3035349C2 (en) 1980-09-19 1980-09-19 Plant for the evaporation of liquid natural gas
DE3035349 1980-09-19

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DE3035349C2 (en) 1985-06-27
DE3168877D1 (en) 1985-03-28

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