WO2009153145A1 - Dispositif servant au mélange de liquide et de vapeur, et procédé pour l'évaporation d'un fluide avec le mélange - Google Patents

Dispositif servant au mélange de liquide et de vapeur, et procédé pour l'évaporation d'un fluide avec le mélange Download PDF

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Publication number
WO2009153145A1
WO2009153145A1 PCT/EP2009/056423 EP2009056423W WO2009153145A1 WO 2009153145 A1 WO2009153145 A1 WO 2009153145A1 EP 2009056423 W EP2009056423 W EP 2009056423W WO 2009153145 A1 WO2009153145 A1 WO 2009153145A1
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WIPO (PCT)
Prior art keywords
liquid
fluid
evaporated
steam
heat
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Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Ceased
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PCT/EP2009/056423
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German (de)
English (en)
Inventor
Volker Brondke
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TGE Gas Engineering GmbH
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TGE Gas Engineering GmbH
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Publication date
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Publication of WO2009153145A1 publication Critical patent/WO2009153145A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • F17C2221/01—Pure fluids
    • F17C2221/014—Nitrogen
    • 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
    • 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
    • F17C2223/0107—Single phase
    • F17C2223/0115—Single phase dense or supercritical, i.e. at high pressure and high density
    • 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
    • F17C2223/033—Small pressure, e.g. for liquefied gas
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/01—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the phase
    • F17C2225/0107—Single phase
    • F17C2225/0123—Single phase gaseous, e.g. CNG, GNC
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/033—Small pressure, e.g. for liquefied gas
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/035—High pressure, i.e. between 10 and 80 bars
    • 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
    • F17C2225/00—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel
    • F17C2225/03—Handled fluid after transfer, i.e. state of fluid after transfer from the vessel characterised by the pressure level
    • F17C2225/036—Very high pressure, i.e. above 80 bars
    • 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
    • F17C2227/0302—Heat exchange with the fluid by heating
    • F17C2227/0309—Heat exchange with the fluid by heating using another fluid
    • F17C2227/0323—Heat exchange with the fluid by heating using another fluid in a closed loop
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/02—Mixing fluids
    • F17C2265/022—Mixing fluids identical fluid
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/05—Regasification
    • 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
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0102—Applications for fluid transport or storage on or in the water
    • F17C2270/0105—Ships
    • 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
    • F17C2270/00—Applications
    • F17C2270/01—Applications for fluid transport or storage
    • F17C2270/0134—Applications for fluid transport or storage placed above the ground
    • F17C2270/0136—Terminals

Definitions

  • the invention relates to a method for the evaporation of a fluid, in particular natural gas in the liquefied or supercritical state.
  • the temperature of the fluid to be evaporated is low, and in particular less than -50 0 C. Whenever liquid gas is mentioned below, it can also be meant the supercritical state.
  • the invention further relates to a device which is used for the evaporation.
  • Natural gas is transported at very low temperatures of typically - 1 60 0 C, for example, by ship.
  • LNG liquefied natural gas
  • LNG may be exposed to pressure equal to atmospheric pressure.
  • LNG to be evaporated can also be exposed to pressures of 80 to 1 40 bar and thus be in the supercritical state.
  • OVR for the vaporization of LNG.
  • the fluid to be vaporized is pumped up in a vertically positioned tube.
  • an existing example of seawater liquid film is directed down the outside of the tube.
  • chlorine has to be added to the water in order to prevent deposits from forming on the pipe. The problem is that after returning the water to the sea, the chlorine must be removed again.
  • the use of an ORV is not allowed for the vaporization of LNG or that Seawater as well as the entire plant must be treated to kill algae and microorganisms such as mussels. So there are also legal problems to evaporate LNG with an OVR.
  • Transfer of heat in a heat exchanger by condensation of steam requires relatively large heat transfer surfaces to be provided to achieve the required heat exchange.
  • the then required heat transfer surfaces are already significantly smaller compared to the case that heat is transferred solely by cooling a fluid in a heat exchanger. Accordingly, expensive and bulky is such a technical solution.
  • Another problem is that for the operation of a heat exchanger regularly maximum temperature differences are to be observed, which between the im Heat exchanger media may occur, so as not to damage the heat exchanger.
  • the object of the invention is to evaporate liquid gas at low cost and to provide a particularly advantageous device for this purpose.
  • heat is transferred by heat exchange from a circulated liquid to the fluid to be evaporated and in particular to LNG.
  • part of the circulated liquid is evaporated.
  • the vaporized part is mixed with the other part of the recirculating liquid, thus heating the circulated liquid as a whole.
  • the now heated in total, circulated liquid is then used again to exchange heat with the fluid to be evaporated, so as to sufficiently heat the fluid to be evaporated.
  • the fluid to be evaporated has temperatures substantially below the freezing point of water, even if the water should have additives that lower the freezing point. Therefore, the temperature of the evaporating fluid is initially in particular less than -50 0 C.
  • the method according to the invention utilizes storing and releasing energy in the form of latent heat. This ensures that the amount of liquid required for the heat exchange can be substantially lower compared to the case in which only liquid is circulated for the purpose of heat transfer.
  • the volume of one for the Evaporation used device can therefore be relatively small. Only relatively small pumping capacities have to be used in the method according to the invention since relatively little liquid has to be circulated. Pipe diameters for guiding the recirculating liquid can be relatively small. Overall, this results in significant cost savings compared to the case in which only liquid is circulated in order to transfer the heat required for evaporation.
  • Condensation temperature would liquefy steam. It can therefore be easily avoided by permissible temperature differences between two streams using the invention technical problems that can occur in a heat exchanger due to excessive temperature differences and consequent inadmissible material loads between two introduced fluids.
  • a liquid is circulated that freezes only at such a low temperature that there is no fear that the recirculated liquid freezes when heat is exchanged with the fluid to be evaporated.
  • the melting point of the recirculated liquid is therefore in one embodiment of the invention less than -100 ° C., preferably less than -150 ° C.
  • Prop ⁇ n having a melting point of - 1 87, 7 0 C is therefore preferred to recycle.
  • An icing of the propane is excluded when LNG is evaporated, which was previously cooled to typical temperatures of, for example - 1 60 0 C.
  • the liquid propane leaves one
  • Heat exchanger then it is typically approx. - 1 35 ° C cold. At this temperature, propane does not freeze, even if propane is exposed to a pressure of 3 to 4 bar. Liquid propylene is also suitable as a fluid, which is recycled.
  • the liquid to be recycled is heated to a temperature of from -10 0 C to -30 0 C, before this liquid is used for the evaporation of the fluid to be evaporated.
  • This is especially the case when the fluid to be vaporized is LNG.
  • a heat exchanger used for the evaporation is not exposed to large temperature differences. It is also possible, for example, to heat propane to this temperature and to ensure that propane is liquid at this temperature by providing a suitable pressure of, in particular, 3 bar to 4 bar.
  • a plate heat exchanger is used to transfer heat from the liquid to be circulated to the fluid to be evaporated.
  • a plate heat exchanger can be comparatively small.
  • a pump is preferably arranged after the transfer of heat to the fluid to be evaporated and before heating the liquid, which causes the transport of the liquid to be recycled in the circuit. If the recirculated liquid leaves a heat exchanger which has been used for heat transfer to a fluid to be evaporated, and if the liquid has not yet been reheated, the liquid particularly reliably contains no vaporous constituents. It This is the most reliable way to avoid the disadvantages that can arise when pumping when steam enters a pump.
  • Evaporation of a part of the liquid to be recirculated with the other part of the liquid reunited by either the liquid atomized and introduced into the vapor or the vapor in the form of a plurality of bubbles is introduced into the liquid.
  • particularly large contact areas between the liquid and the steam are used.
  • Konta ktrios the faster the heat between the steam and the liquid can be replaced.
  • perforated tubes are used in one embodiment of the invention. Through the perforations through the steam is introduced into the liquid. This is achieved simply and inexpensively, that the steam in the form of many small bubbles is introduced into the liquid. This contributes to the reasons mentioned above to be able to evaporate inexpensively.
  • a typical, suitable diameter of the holes of the perforations is 2 to 5 mm.
  • one or more double-walled tubes with perforated inner walls are provided to mix vapor with liquid. In the inner tube of such a double-walled tube of the vapor or liquid is introduced and, conversely, the liquid or vapor in the annular gap between the two walls of the tube.
  • the steam introduced into the jacketed tube is pumped through the perforations into the liquid.
  • space can be transferred heat from the steam to the liquid with a particularly high efficiency.
  • steam is introduced into the inner tube and pumped into the annular gap through the perforations in order to mix in the annular gap with the liquid introduced here and thus to transfer heat.
  • a proven distance between two walls of a double-walled pipe is typically 40 mm to 80 mm.
  • the dimensionless WEBER -al modified FROUDE number used as a criterion for secondary particle formation.
  • the WEBER number describes the ratio of inertial force to surface force, while the FROUDE number represents the ratio of inertial force to gravity.
  • the critical WEBER or FROUDE number represents at the same time an important operating parameter for perforated trays.
  • the WEBER number is at least 2 with a FROUDE number of at least 0.37, a uniform flow through the perforated tray and the Ingress of liquid phase into the gas space avoided (rain out). Therefore, a farm with a Weber number of at least 2 and a fondue of at least 0.37 has proven itself.
  • the hole density of a perforated wall decreases when the liquid flows in the same direction on the other side of the wall. For if steam passes through the holes in the liquid, the liquid heats up increasingly in the flow direction. The warmer the liquid becomes, the longer a vapor or gas bubble must be carried in the liquid before the entrained vapor bubbles collapse.
  • the decreasing hole density ensures that there are not as many vapor bubbles in a volume of liquid at the same time that these vapor bubbles combine and further effective heat exchange is prevented when the temperature of the liquid rises too high.
  • the distribution of the holes is chosen and the method is carried out so that the liquid during the introduction of steam has a temperature which is at least 1 0 0 C below the boiling point. By adhering to this upper temperature limit is avoided that steam bubbles unite disadvantageously in the liquid.
  • the hole density decreases in particular logarithmically, and particularly preferably according to a natural logarithm from
  • This embodiment of the invention helps to minimize required pumping power.
  • the steam is pumped from a tube in a star shape to the double-walled tubes.
  • an optimal gas distribution can be achieved on a plurality of double-walled tubes used with minimal space requirements.
  • the efficiency of the heat exchange is further increased. From a central feeder starting the further star-shaped feed is such that always the same distance is covered to get into a double-walled tube. If the flow cross-sections of the star-shaped feeders are the same, there are basically identical pressure conditions in the double-walled tubes, which is preferable.
  • Double-walled tubes with perforated inner walls are connected in the flow direction with a tube which has deflection means inside. Double-walled tubes are combined in such a way that the steam introduced into a double-walled tube is completely or at least substantially completely collapsed after leaving the tube and thus the space required for further transport has been significantly reduced.
  • the pipe By deflecting the recirculated liquid is swirled once again, so as to ensure once again that the gas is completely converted into the liquid state.
  • the pipe is again a double-walled pipe.
  • the liquid is first supplied to the inner tube, in which the deflection devices are housed. After passing through the inner tube, the liquid enters the annular gap. In this way it can be achieved structurally in a particularly space-saving manner, that a device for heating the recirculated liquid on one end side yakloom the liquid to be circulated and is directed out on another end face.
  • a heat exchanger in which the fluid to be evaporated is introduced in opposite directions.
  • heat is transferred from the recirculating liquid to the fluid to be evaporated.
  • a heat exchanger is used, preferably a plate heat exchanger.
  • a plate heat exchanger has small dimensions and large transfer surfaces. The energy for the transfer to the vapor phase, for example, by particularly opposite supply of water, such as seawater or wastewater in the plate heat exchanger.
  • the part of the recirculated liquid to be evaporated is preheated in one embodiment of the invention. This is done in one embodiment of the invention by mixing a portion of the vaporized liquid with the portion of the liquid which is subsequently vaporized. The preheating is done so before a part of the circulated liquid is evaporated. Part of the circulated liquid is preheated after heat has been transferred to the fluid to be evaporated and subsequently the liquid has been divided.
  • the preheating is preferably carried out so that the affected part of the liquid is brought to a temperature of more than -50 0 C, preferably to a temperature of more than -40 0 C, so as to reliably avoid icing of the subsequent heat exchanger.
  • the liquid is preferably not heated to temperatures of more than -20 0 C, so as to avoid vaporous components.
  • the liquid is supplied to a pump which generates an overpressure of gas to liquid in a subsequent device in which steam is mixed with liquid.
  • a 6m to 8m long device with a diameter of 2m to 3m can be provided by the invention, with the approx. 32MW to 37MW evaporation power for approx. 200t / h LNG is available.
  • the heated fluid is preferably supplied to a further heat exchanger in order to heat the fluid to above 0 ° C., for example to room temperature.
  • a plate heat exchanger is used by the propane is circulated. Propane receives its heat energy, for example via a second plate heat exchanger through water. But it could also be used due to the then relatively low temperatures of the fluid, a heat exchanger, is passed directly through the water, since the risk of icing is relatively low, or it could be used a different heating medium.
  • the entire structure for vaporizing a fluid requires significantly less space compared to the space required by the prior art described above to convert LNG to the vapor state.
  • the smaller construction saves manufacturing and storage costs.
  • the total required pump power can be significantly reduced compared to the prior art. For example, compared to the case where liquid propane evaporates a fluid to be vaporized without completely or partially vaporizing the propane, the required pumping power can be reduced by 50%.
  • LNG is to be evaporated.
  • the invention eig net also for the evaporation of other cryogenic liquids such as ethylene or ethane.
  • the invention can be realized in an embodiment advantageously in the power plant area.
  • water is evaporated in order to drive one or more turbines with the evaporated water. After steam has driven a turbine and done so work, the steam is converted into water, to be able to lead the water or water vapor in the so-called primary circuit can.
  • prior art condensation is accomplished inter alia by spraying or spraying circulating water into the water vapor after the steam has passed the turbine and performed work. The water is recycled because it is specially treated water called deionate.
  • part of the water to be evaporated is used to spray it into the steam which has already done work.
  • the vapor thus condensed, together with the water used for the condensation, is returned to the tank or tank containing the water to be evaporated.
  • the water to be evaporated is preheated so desired at the same time. Preheated water in the tank is vaporized to drive a turbine with the steam.
  • the steam is introduced after leaving a turbine into the liquid with a device according to the invention.
  • the costs can be significantly reduced compared to the prior art.
  • the costs that have to be spent on the required devices are reduced.
  • the pumping power drops must be spent to condense the steam that has done work.
  • the invention is also used, for example, in the context of providing district heating. Heat from the invention
  • Primary fluid circuit, with which turbines are driven, are delivered to a secondary fluid circuit.
  • This secondary circuit is heated and so a fluid, usually water, transported to the consumer to use the heat thus transported for heating.
  • steam is now generated in the secondary circuit with the aid of the primary circuit and heat exchangers.
  • This steam is typically very hot, and in particular hotter than 21 0 0 C.
  • the temperature of the water may not exceed 90 0 C. It is therefore necessary to convert the generated water vapor of the secondary circuit into water and to adjust water temperatures below 90 0 C before the water reaches the private consumer.
  • the invention is advantageously used.
  • a heat exchange takes place, for example via tube bundle exchanger to obtain 90 ° warm water. It is now cheaper to introduce the water vapor according to the invention in water, so to condense the water vapor on one side and to bring the water temperature to 90 0 C on the other side. Again, the amount of water to be circulated can be minimized, which saves pumping power. In addition, the equipment costs are lower compared to the described prior art.
  • the invention can be advantageously used in heat exchangers to heat a liquid by means of steam cost-effective or to condense steam cost.
  • the electricity is typically generated in the chemical plant and used waste heat to use this for the various chemical manufacturing processes.
  • desired secondary circuit temperatures and to pass the appropriately heated liquid, preferably water, to the various stations for the production of products requiring heat.
  • the invention is advantageously used to set the respectively desired temperatures or temperature ranges.
  • water vapor from the turbine to generate electricity in a chemical plant this is then performed in the primary circuit.
  • the resulting waste heat is used to heat a secondary cycle of a fluid.
  • the respectively desired temperatures are now set cost-effectively and thus temperature-controlled fluid is forwarded to the desired method.
  • the arrangement according to the invention is preferably arranged horizontally so that perforated tubes of the arrangement run horizontally. If there are a plurality of perforated tubes arranged in a star shape, then it can be achieved that each of these tubes flows through in the same way. For vertical installation, this would be difficult to achieve due to gravity. It is therefore easier to optimize the overall flow behavior in a horizontal position.
  • FIG 1 shows in section a device according to the invention, with the latent heat of a vapor with high efficiency of a liquid is supplied without having to provide a large volume for it.
  • a central channel 1 with a relatively large diameter, is introduced into the steam, branch off a plurality of pipe joints 2 star-shaped.
  • the steam is introduced into inner tubes 3 of double-walled tubes 4.
  • the inner walls 5 of the double-walled tubes 4 are perforated.
  • the density of the holes decreases in the flow direction of the steam according to a natural logarithm.
  • In the annular gap 7 of each double-walled pipe liquid is introduced lines shown in Figure 2 to 27 in the same direction as the flow direction of the vapor in the associated inner tubes 3.
  • each double-walled tube 3 Between the liquid in one of the annular gaps and the steam in the associated inner tube 3, there is such a pressure difference that the steam passes through the perforation into the liquid.
  • the liquid contents are passed in pairs to another double-walled tube 8 and indeed into the inner tube 9 inside.
  • each inner tube 9 In each inner tube 9 are means for swirling 26 (see Figure 2) of the liquid introduced. If the liquid has passed through the inner tube 9, it flows back through the annular gap 10. There is then a liquid which has been heated in a relatively small volume by the steam, or the vapor has been liquefied in a relatively small volume with high efficiency.
  • liquid natural gas is stored in a tank, a certain amount always evaporates. This part must be liquefied again.
  • a recondenser is used for this purpose. The resulting vapor is fed to the recondenser. Next liquid natural gas is supplied and liquefied by heat exchange of the steam again.
  • a typical height of a recondenser is 1 5m. If, instead of the known recondenser, a device such as that shown in FIG. 1 is used in such a way that the undesired vaporized part is liquefied, the height of such a device can be reduced to V 3 . It saves so much space and thus costs.
  • a device as shown in Figure 1 can be used to supply and thus package LNG nitrogen.
  • a device, as shown in FIG. 1 can always be advantageously used when steam is to be mixed into a liquid and liquefied.
  • FIG. 2 shows a longitudinal section of the device shown in FIG.
  • the wavy filling arrows indicate the flow direction of the liquid.
  • the arrows without filling illustrate the flow of steam.
  • liquid and vapor are introduced separately.
  • the heated liquid can be removed. It is shown that liquid passes through feeds 27 to annular gaps and can finally be removed on the opposite side via an outlet 28.
  • the walls of the tube 9 shown in Figure 2 are not perforated, so impermeable.
  • Figure 3 illustrates the evaporation of fluid LNG, which is introduced via a line 1 1 usually in the supercritical, very cold state (typically - 1 60 0 C) in a plate heat exchanger 1 2 and this with a temperature of approx. -20 0 C leaves via a line 1 3.
  • 1 2 liquid propane flows through a feed line 1 4 into the plate heat exchanger at a temperature of approx. - 1 0 0 C into it.
  • the liquid propane leaves the plate heat exchanger at a temperature of approx. - 1 35 ° C via a line 1 5 and thus passes in the guaranteed liquid state to a pump 1 6, which ensures that the propane flows through a circuit.
  • a portion of the liquid propane is introduced via a line 1 7 in a device 1 8 according to Figures 1 and 2.
  • the other part of the liquid propane is supplied to a device 20, as shown in Figures 1 and 2.
  • the liquid propane is heated to a temperature of -35 ° C. Thanks to a prevailing pressure of 3 to 4 bar, the propane heated to -35 ° C. leaves the device 20 reliably in the liquid state and thus reaches a pump 21.
  • the preheated, liquid propane is pumped into a plate heat exchanger 22.
  • the preheated propane evaporated with the help of seawater, which is passed through the heat exchanger 22 opposite.
  • the propane vapor emerging from the plate heat exchanger 22 is in part introduced via a line 23 into the device 20 and mixed with the liquid propane, whereby the liquid propane is preheated.
  • the other part of the propane vapor is introduced via a line 24 in the device 1 8 and mixed here with the liquid propane, which at a temperature of approx. - 1 35 ° C in the device 1 8 is initiated.
  • the pump 21 ensures that the introduced into the devices 1 8 and 21 propane gas is under higher pressure compared to the introduced liquid propane gas. Liquid propane gas leaves the device 1 8 at a temperature of - 1 0 0 C and thus enters the heat exchanger 1 second
  • the heated in the plate heat exchanger 1 2 LNG is fed via the line 1 3 a further plate heat exchanger 25 and here indirectly or directly with the help of seawater to above 0 0 C heated.
  • the invention can be realized in an embodiment advantageously in the power plant area.
  • water is evaporated in order to drive turbines with the evaporated water. After the evaporation of the water, this must be converted back into water, in order to be able to lead it in the cycle - primary cycle called.
  • the condensation is effected, inter alia, by circulating water is injected into the Wasserdam pf after the steam has passed the turbine. The water is recycled because it is specially treated water called dionate. Therefore, part of the water to be evaporated is used to spray it into the steam that has already done its work. The steam condensed in this way is combined with that for the
  • the water to be evaporated is preheated so desired at the same time.
  • the in the container or Tank located, preheated water is partially evaporated to drive a turbine with the steam.
  • the steam is introduced after leaving a turbine into the liquid with a device according to the invention.
  • the costs can be significantly reduced compared to the prior art.
  • the costs that have to be spent on the required devices are reduced.
  • the pumping power that has to be expended in order to condense the steam has done the work.
  • the invention is also used, for example, in the context of providing district heating. Heat from the invention
  • Primary fluid circuit, with which turbines are driven, are delivered to a secondary fluid circuit.
  • This secondary circuit is heated and so a fluid, usually water, transported to the consumer to use the heat thus transported for heating.
  • steam is now generated in the secondary circuit with the aid of the primary circuit and heat exchangers.
  • This steam is typically very hot, and in particular hotter than 21 0 0 C.
  • the temperature of the water may not exceed 90 0 C. It is therefore necessary to convert the generated water vapor of the secondary circuit into water and adjust water temperatures below 90 0 C before the water reaches the private consumer. Should now the generated water vapor in 90 0 C warm water to be converted, so again the invention is advantageously used.
  • a heat exchange takes place, for example via tube bundle exchanger to obtain 90 ° warm water.
  • the invention can be advantageously used in heat exchangers to heat a liquid by means of steam cost-effective or to condense steam cost.
  • the invention is advantageously used to adjust the respective desired temperatures or temperature ranges.
  • water vapor from the turbine to generate electricity in a chemical plant this is then performed in the primary circuit.
  • the resulting waste heat is used to heat a secondary cycle of a fluid.
  • the respectively desired temperatures are now set cost-effectively and thus temperature-controlled fluid is forwarded to the desired process.
  • the arrangement according to the invention is preferably arranged horizontally so that perforated tubes of the arrangement run horizontally. Is there a Plurality of star-shaped perforated pipes, so can be achieved so that each of these tubes is flowed through in the same way, With vertical placement this would be hard to achieve due to gravity. It is therefore easier to optimize the flow behavior in a horizontal position.

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Abstract

L'invention concerne un procédé pour l'évaporation d'un fluide, en particulier de gaz naturel à l'état liquéfié ou surcritique. La température du fluide à évaporer est faible, à savoir notamment inférieure à -50°C. Dans ce qui suit, la notion de gaz liquéfié impliquera donc également l'état surcritique. L'invention concerne en outre un dispositif qui est utilisé pour l'évaporation. L'invention a pour but d'évaporer un gaz liquide de manière économique et, à cet effet, de développer un dispositif particulièrement avantageux. Le procédé de l'invention qui est en conséquence basé sur un échange de chaleur, est caractérisé en ce que la chaleur est transférée d'un liquide circulant dans un circuit, au fluide à évaporer, et notamment au LNG. Après échange de chaleur, une partie du liquide circulant dans le circuit est évaporée. La partie évaporée est mélangée avec l'autre partie du liquide circulant dans le circuit, de sorte que l'ensemble du liquide en circulation dans le circuit est réchauffé. Le liquide ainsi réchauffé est par la suite utilisé pour échanger de la chaleur avec le fluide à évaporer, de manière à évaporer ledit fluide à évaporer.
PCT/EP2009/056423 2008-06-19 2009-05-27 Dispositif servant au mélange de liquide et de vapeur, et procédé pour l'évaporation d'un fluide avec le mélange Ceased WO2009153145A1 (fr)

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DE200810002531 DE102008002531A1 (de) 2008-06-19 2008-06-19 Vorrichtung für das Mischen von Flüssigkeit und Dampf sowie Verfahren für das Verdampfen eines Fluids mit der Mischung
DE102008002531.3 2008-06-19

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Cited By (4)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102181955A (zh) * 2011-03-18 2011-09-14 开平市冠威乳胶设备制造有限公司 一种用于超细高弹乳胶丝生产的热水系统热能回收装置
WO2013020907A1 (fr) 2011-08-05 2013-02-14 Somfy Sas Procédé de commande d'un écran et actionneur adapté pour un tel procédé
WO2013020908A1 (fr) 2011-08-05 2013-02-14 Somfy Sas Procédés de configuration et de commande d'un groupe d'écrans et actionneur adapté pour un tel procédé de commande
WO2013020906A1 (fr) 2011-08-05 2013-02-14 Somfy Sas Procédé de commande d'un écran et actionneur adapté pour un tel procédé

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB202408642D0 (en) * 2024-06-17 2024-07-31 Rolls Royce Plc Method and apparatus for heating a flow of hydrogen
WO2026022276A1 (fr) * 2024-07-24 2026-01-29 Ikm Flux As Vaporisateur pour vaporiser un liquide tel que du gaz naturel liquéfié et son procédé de fabrication

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3164957A (en) * 1961-03-10 1965-01-12 Republic Aviat Corp Thermal energy converting system
GB1451767A (en) * 1975-05-29 1976-10-06 Heat Res Corp Method of vaporising liquefied natural gas
US4238296A (en) * 1978-05-17 1980-12-09 Occidental Research Corporation Process of desalination by direct contact heat transfer
EP0429425A1 (fr) * 1989-11-17 1991-05-29 Union Carbide Industrial Gases Technology Corporation Cylindre ayant des caractéristiques de mÀ©lange améliorés
DE4210738A1 (de) * 1992-04-01 1992-12-24 Edwin Schmidt Verfahren und vorrichtungen zur kaltvergasung kaelteverfluessigter gase
US5325894A (en) * 1992-12-07 1994-07-05 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied natural gas
US20040182082A1 (en) * 2002-12-26 2004-09-23 Saranchuk Theodore Charles Low temperature heat engine
US20050274126A1 (en) * 2004-06-15 2005-12-15 Baudat Ned P Apparatus and methods for converting a cryogenic fluid into gas
EP1803990A1 (fr) * 2006-01-02 2007-07-04 Linde Aktiengesellschaft Dispositif destiné au stockage de médias en forme de gaz

Family Cites Families (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH08338692A (ja) 1995-06-13 1996-12-24 Tokyo Gas Co Ltd オープンラック式気化装置
DZ2528A1 (fr) 1997-06-20 2003-02-01 Exxon Production Research Co Conteneur pour le stockage de gaz natural liquéfiesous pression navire et procédé pour le transport de gaz natural liquéfié sous pression et système de traitement de gaz natural pour produire du gaz naturel liquéfié sous pression.
US8069677B2 (en) 2006-03-15 2011-12-06 Woodside Energy Ltd. Regasification of LNG using ambient air and supplemental heat

Patent Citations (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3164957A (en) * 1961-03-10 1965-01-12 Republic Aviat Corp Thermal energy converting system
GB1451767A (en) * 1975-05-29 1976-10-06 Heat Res Corp Method of vaporising liquefied natural gas
US4238296A (en) * 1978-05-17 1980-12-09 Occidental Research Corporation Process of desalination by direct contact heat transfer
EP0429425A1 (fr) * 1989-11-17 1991-05-29 Union Carbide Industrial Gases Technology Corporation Cylindre ayant des caractéristiques de mÀ©lange améliorés
DE4210738A1 (de) * 1992-04-01 1992-12-24 Edwin Schmidt Verfahren und vorrichtungen zur kaltvergasung kaelteverfluessigter gase
US5325894A (en) * 1992-12-07 1994-07-05 Chicago Bridge & Iron Technical Services Company Method and apparatus for fueling vehicles with liquefied natural gas
US20040182082A1 (en) * 2002-12-26 2004-09-23 Saranchuk Theodore Charles Low temperature heat engine
US20050274126A1 (en) * 2004-06-15 2005-12-15 Baudat Ned P Apparatus and methods for converting a cryogenic fluid into gas
US20080053110A1 (en) * 2004-06-15 2008-03-06 Baudat Ned P Apparatus And Methods For Converting A Cryogenic Fluid Into Gas
EP1803990A1 (fr) * 2006-01-02 2007-07-04 Linde Aktiengesellschaft Dispositif destiné au stockage de médias en forme de gaz

Cited By (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102181955A (zh) * 2011-03-18 2011-09-14 开平市冠威乳胶设备制造有限公司 一种用于超细高弹乳胶丝生产的热水系统热能回收装置
CN102181955B (zh) * 2011-03-18 2013-07-10 开平市嘉仁乳胶设备制造有限公司 一种用于超细高弹乳胶丝生产的热水系统热能回收装置
WO2013020907A1 (fr) 2011-08-05 2013-02-14 Somfy Sas Procédé de commande d'un écran et actionneur adapté pour un tel procédé
WO2013020908A1 (fr) 2011-08-05 2013-02-14 Somfy Sas Procédés de configuration et de commande d'un groupe d'écrans et actionneur adapté pour un tel procédé de commande
WO2013020906A1 (fr) 2011-08-05 2013-02-14 Somfy Sas Procédé de commande d'un écran et actionneur adapté pour un tel procédé

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