EP3397912B1 - Verfahren und wärmeaustauscher zur rückgewinnung von kälte bei der regasifizierung tiefkalter flüssigkeiten - Google Patents

Verfahren und wärmeaustauscher zur rückgewinnung von kälte bei der regasifizierung tiefkalter flüssigkeiten Download PDF

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Publication number
EP3397912B1
EP3397912B1 EP16742154.4A EP16742154A EP3397912B1 EP 3397912 B1 EP3397912 B1 EP 3397912B1 EP 16742154 A EP16742154 A EP 16742154A EP 3397912 B1 EP3397912 B1 EP 3397912B1
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EP
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Prior art keywords
coiled
coiled tubes
heat exchanger
tubes
intermediate medium
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EP16742154.4A
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German (de)
English (en)
French (fr)
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EP3397912A1 (de
Inventor
Rainer Braun
Peter Otto
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Eco Ice Kalte GmbH
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Eco Ice Kalte GmbH
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    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/0066—Multi-circuit heat-exchangers, e.g. integrating different heat exchange sections in the same unit or heat-exchangers for more than two fluids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D7/00—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall
    • F28D7/02—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled
    • F28D7/022—Heat-exchange apparatus having stationary tubular conduit assemblies for both heat-exchange media, the media being in contact with different sides of a conduit wall the conduits being helically coiled the conduits of two or more media in heat-exchange relationship being helically coiled, the coils having a cylindrical configuration
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F28—HEAT EXCHANGE IN GENERAL
    • F28D—HEAT-EXCHANGE APPARATUS, NOT PROVIDED FOR IN ANOTHER SUBCLASS, IN WHICH THE HEAT-EXCHANGE MEDIA DO NOT COME INTO DIRECT CONTACT
    • F28D21/00—Heat-exchange apparatus not covered by any of the groups F28D1/00 - F28D20/00
    • F28D2021/0019—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for
    • F28D2021/0061—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications
    • F28D2021/0066—Other heat exchangers for particular applications; Heat exchange systems not otherwise provided for for phase-change applications with combined condensation and evaporation

Definitions

  • the invention relates to the recovery of cold in the regasification of cryogenic liquids, in particular liquefied natural gas (LNG, Liquefied Natural Gas at -162 ° C and 1 bar atmospheric pressure), liquefied nitrogen (LN2) and liquefied oxygen (LO2).
  • LNG liquefied natural gas
  • LN2 liquefied nitrogen
  • LO2 liquefied oxygen
  • process characteristics are specified in connection with a heat exchanger for realizing the method.
  • the heat exchanger is designed for, although in comparison to the fuel energy relatively small, yet valuable cooling capacity in the range below 100 kW and is characterized by simple design features and ease of use, which allow the refrigeration capacity reasonably low investment.
  • Natural gas can be transferred under atmospheric pressure after cooling to -162 ° C and subsequent removal of the heat of condensation from the gaseous to the liquid phase.
  • the reduction of the volume is connected to six hundredths of the value given at 1.013 bar and 15 ° C.
  • Liquefied natural gas can thus be stored in an attractive manner and transported over long distances.
  • the equally costly and value-adding process chain to be realized ranges from extraction and processing via liquefaction, storage, long-distance transport with tankers, re-storage in large tanks and repeated transport to the user until regasification.
  • the end of this chain is very often a so-called satellite system, namely a double-walled, vacuum-insulated LNG storage without liquefaction.
  • the satellite system has a regasification device, usually an atmospheric evaporator with vertical longitudinal tubes, at which liquefied natural gas, hereinafter referred to as LNG, is vaporized and overheated to ambient temperature, while the required heat from the ambient air is supplied by free convection.
  • a regasification device usually an atmospheric evaporator with vertical longitudinal tubes, at which liquefied natural gas, hereinafter referred to as LNG, is vaporized and overheated to ambient temperature, while the required heat from the ambient air is supplied by free convection.
  • the cold of the LNG is transferred to a liquid refrigerant, which is to be used down to the temperature level of about -60 ° C, without pumping phase change and thus remains safe.
  • a liquid refrigerant which is to be used down to the temperature level of about -60 ° C, without pumping phase change and thus remains safe.
  • Therminol D12 a synthetic liquid based on aliphatic hydrocarbons.
  • the energy transfer does not take place directly on the liquid refrigerant, but first on an intermediate medium (intermediate fluid) and from this then on the liquid refrigerant.
  • the use of the intermediate medium serves to overcome the large difference in temperature between the low-temperature liquid to be regasified and the refrigerant without the refrigerant cooling too strongly, even to the point of solidification of the same.
  • the heat transfer via this intermediate medium takes place at a selectable intermediate temperature by evaporation and condensation in natural circulation, ie without the use of a pump, in a heat exchanger according to the invention for cooling capacities below 100 kW.
  • This heat exchanger is expediently designed as a cylinder in vertical alignment and closed at the top and bottom by dished ends.
  • the container thus realized contains in the upper part at least one surface heat exchanger for evaporating the cryogenic liquid, for example LNG, and in the lower part at least one further surface heat exchanger for cooling the liquid refrigerant.
  • this is filled with the intermediate medium, preferably propane, which is securely encapsulated.
  • the propane is in the lower part to the level of a boiling liquid and in the upper region above the filling level condensing saturated steam.
  • Both surface heat exchangers are designed as tube helices.
  • the pipe coils associated collecting pipes are useful, with other fastening solutions can be realized.
  • the heat transfer from the refrigerant to be cooled to the liquid intermediate medium can be done on the lower tube coils.
  • the heat transfer from the upper coiled tubing to the deep-frozen liquid to be evaporated is particularly effective because of the long flow path and the resulting on a circular path secondary flow in the interior of the coiled tubing.
  • the largest transport resistance the reduction of which has a particularly positive effect on the entire heat transfer result.
  • the use of a turbulator can further reduce this transport resistance.
  • the cylindrical container is after its evacuation with the intermediate medium, preferably propane, taking into account temperature, density and mass sustainably filled so that the upper tube coils remain free at each subsequent operating state, while the lower tube coils of liquid intermediate medium in the boiling state are completely flooded.
  • the intermediate medium preferably propane
  • This distance can be calculated with the help of the material values of the intermediate medium. It corresponds approximately to the diameter of the coiled tubing.
  • Characteristic properties of the intermediate medium propane are the following: At 25 ° C, the pressure of the propane (saturated steam and liquid in the boiling state are in phase equilibrium.) About 9.6 bar. The density of the liquid is then about 492 kg / m 3 .
  • the density of the liquid phase is then about 612 kg / m 3 .
  • the following embodiments are related to the regasification of cryogenic liquefied natural gas LNG (Liquefied Natural Gas) stored in a satellite tank farm.
  • LNG Liquified Natural Gas
  • the inventive method for recovering cold from liquefied natural gas (LNG) in conjunction with heat exchangers for brine temperature levels above -60 ° C and for cooling capacities in the range below 100 kW explained in more detail with reference to drawings.
  • the heat exchangers used differ in their design.
  • FIG. 1 An inventive heat exchanger is in FIG. 1 shown as a section along its vertical axis system. It is a cylindrical container 1 in vertical orientation, which is closed with an upper and a lower dished bottom 2 and 3 and is completely covered with an insulation 5. In the region of the upper dished bottom 2, a coiled tubing 6 and at the lower dished bottom 3, a coiled tubing 7 is arranged directly or indirectly in each case in freely projecting into the container interior. The attachment to the container 1 is realized only on one side. For the purpose of heat transport within the hermetically sealed container 1, this is filled with the intermediate medium 8, namely propane 8, which is thus securely encapsulated.
  • the intermediate medium 8 namely propane 8
  • the level 9 of the liquid intermediate medium 8 in the container 1 is adjusted so that the upper tube coil 6 is surrounded in each operating state of gaseous intermediate medium 8.1 and the lower tube coil 7 is flooded with liquid intermediate medium 8.2.
  • an appropriate distance of approximately the diameter of the coiled tubing 6 or 7 is present between the two coiled tubing 6 and 7 and the corresponding mass of the intermediate medium 8 is filled into the container.
  • the container 1 and the tube coils 6 and 7 are advantageously made of stainless steel. This guarantees sufficient cryogenic toughness and high corrosion resistance.
  • the heat transfer from the condensing propane saturated steam 8.1 to the deep-frozen liquid LNG to be regasified is thus effected via the upper coiled tubing 6. As already mentioned, this protrudes freely from above into the interior of the container. This has the advantage that mechanical stresses due to the large temporal temperature changes occurring during operation are sufficiently avoided.
  • the heat transfer from the coolant to be cooled to the liquid, boiling propane 8.2 takes place at the lower coiled tubing. 7 Since the lower coiled tubing 7 is mechanically connected in the same way to the lower region of the container, the described advantages of this attachment result analogously to the upper coiled tubing 6.
  • As a refrigerant advantageously Therminol D12 is used.
  • FIG. 2 Another inventive heat exchanger is in FIG. 2 also shown as a section along its vertical axis system. It differs from the above-described heat exchanger in that both the coiled tubing 6 and the coiled tubing 7 are present in multiple arrangement in the container 1 in otherwise analogous construction. In the example chosen, seven tube coils 6 and 7 are arranged in each case. All other features are taken apart from structural adjustments. It has proved to be advantageous to design the inflow 10 of the LNG directly with the interposition of a distributor 15 and to realize the outflow 11 of the regasified LNG via a collecting pipe 16 in the upper part of the container 1.
  • the inflow 12 of the refrigerant to the coiled tubing 7 is also carried out with the interposition of a manifold 15 directly, while the drain 13 is realized via a further manifold 16 in the lower part of the container 1.
  • the two manifolds 16 may alternatively be arranged outside the container 1. It is recommended to use the headers 16 for each one-sided attachment of the coiled tubing 6 and 7 on the container 1. Depending on the conditions of use, the upper and / or lower tube coils 6 and 7 can be connected individually or in bundles.
  • the described heat exchangers according to the invention enable effective heat transfer from the cooling medium to be cooled to the boiling intermediate medium 8.2 in the area of the lower coiled tubing or tube spirals 7 and from the condensing, gaseous intermediate medium 8.1 to the cryogenic liquid to be evaporated in the area of the upper coiled tubing or coiled tubing 6.
  • the natural circulation of the intermediate medium comes through the dripping of the condensate from the or the upper coiled tubing 6 to conditions.

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  • Engineering & Computer Science (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Heat-Exchange Devices With Radiators And Conduit Assemblies (AREA)
EP16742154.4A 2015-12-28 2016-06-17 Verfahren und wärmeaustauscher zur rückgewinnung von kälte bei der regasifizierung tiefkalter flüssigkeiten Active EP3397912B1 (de)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
DE102015016889 2015-12-28
DE102016006121.9A DE102016006121A1 (de) 2015-12-28 2016-05-18 Verfahren und Wärmeaustauscher zur Rückgewinnung von Kälte bei der Regasifizierung tiefkalter Flüssigkeiten
PCT/DE2016/000253 WO2017114518A1 (de) 2015-12-28 2016-06-17 Verfahren und wärmeaustauscher zur rückgewinnung von kälte bei der regasifizierung tiefkalter flüssigkeiten

Publications (2)

Publication Number Publication Date
EP3397912A1 EP3397912A1 (de) 2018-11-07
EP3397912B1 true EP3397912B1 (de) 2019-11-13

Family

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EP16742154.4A Active EP3397912B1 (de) 2015-12-28 2016-06-17 Verfahren und wärmeaustauscher zur rückgewinnung von kälte bei der regasifizierung tiefkalter flüssigkeiten

Country Status (4)

Country Link
EP (1) EP3397912B1 (zh)
DE (2) DE102016006121A1 (zh)
TW (1) TW201730475A (zh)
WO (1) WO2017114518A1 (zh)

Families Citing this family (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE102017007009A1 (de) 2017-07-25 2019-01-31 Eco ice Kälte GmbH Kälteversorgungsanlage, gekoppelt an die Regasifizierungseinrichtung eines Liquified Natural Gas Terminals
CN109751508B (zh) * 2017-11-02 2021-06-11 浙江三花智能控制股份有限公司 液化天然气气化器
DE102017012125A1 (de) * 2017-12-29 2019-07-04 Eco ice Kälte GmbH Wärmeübertragungseinrichtung für die Kältebereitstellung in Kühlfahrzeugen, deren Kraftfahrzeugmotor mit LNG angetrieben wird
DE102020001338A1 (de) 2020-02-29 2021-09-02 REGASCOLD GmbH Wärmeübertrager für die Rückgewinnung von Kälteleistung aus der Regasifizierung tiefkalter verflüssigter Gase

Family Cites Families (7)

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Publication number Priority date Publication date Assignee Title
US6089022A (en) 1998-03-18 2000-07-18 Mobil Oil Corporation Regasification of liquefied natural gas (LNG) aboard a transport vessel
JP4291459B2 (ja) 1999-06-28 2009-07-08 大阪瓦斯株式会社 熱交換器の徐冷方法及び装置
JP3946398B2 (ja) 2000-01-18 2007-07-18 株式会社神戸製鋼所 中間媒体式気化器及び当該気化器を用いた天然ガスの供給方法
AU2003269731A1 (en) 2002-10-04 2004-04-23 Hamworthy Kse A.S. Regasification system and method
DE102008031041B4 (de) * 2008-06-30 2010-06-02 Aprovis Energy Systems Gmbh Wärmetauscher zur Porzessgasaufbereitung
EP2720767A1 (en) * 2011-06-20 2014-04-23 Praxair Technology, Inc. System and method for cryogenic condensing
DE102011081673A1 (de) 2011-08-26 2013-02-28 Siemens Aktiengesellschaft Verfahren und Anlage zur Regasifizierung von Flüssigerdgas

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
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Publication number Publication date
WO2017114518A1 (de) 2017-07-06
TW201730475A (zh) 2017-09-01
EP3397912A1 (de) 2018-11-07
DE112016006090A5 (de) 2019-01-10
DE102016006121A1 (de) 2017-06-29

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