WO2007011921A2 - Configurations et methodes de production d'energie dans des terminaux de regazification de gnl - Google Patents

Configurations et methodes de production d'energie dans des terminaux de regazification de gnl Download PDF

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Publication number
WO2007011921A2
WO2007011921A2 PCT/US2006/027798 US2006027798W WO2007011921A2 WO 2007011921 A2 WO2007011921 A2 WO 2007011921A2 US 2006027798 W US2006027798 W US 2006027798W WO 2007011921 A2 WO2007011921 A2 WO 2007011921A2
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Prior art keywords
natural gas
vaporizer
vaporized natural
lng
heat
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Ceased
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PCT/US2006/027798
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English (en)
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WO2007011921A3 (fr
WO2007011921B1 (fr
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John Mak
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Fluor Technologies Corp
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Fluor Technologies Corp
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Publication date
Application filed by Fluor Technologies Corp filed Critical Fluor Technologies Corp
Priority to CN200680026102.4A priority Critical patent/CN101238322B/zh
Priority to EP06787671.4A priority patent/EP1904782A4/fr
Priority to US11/917,387 priority patent/US20100030199A1/en
Priority to MX2008000503A priority patent/MX2008000503A/es
Priority to CA2615850A priority patent/CA2615850C/fr
Publication of WO2007011921A2 publication Critical patent/WO2007011921A2/fr
Publication of WO2007011921A3 publication Critical patent/WO2007011921A3/fr
Publication of WO2007011921B1 publication Critical patent/WO2007011921B1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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    • 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
    • F17C7/00—Methods or apparatus for discharging liquefied, solidified, or compressed gases from pressure vessels, not covered by another subclass
    • F17C7/02—Discharging liquefied gases
    • F17C7/04—Discharging liquefied gases 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
    • F17C2223/033—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
    • F17C2225/036—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
    • F17C2227/01—Propulsion of the fluid
    • F17C2227/0128—Propulsion of the fluid with pumps or compressors
    • F17C2227/0135—Pumps
    • 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
    • F17C2227/0306—Heat exchange with the fluid by heating using the same 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
    • 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
    • F17C2227/0311—Air heating
    • 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
    • F17C2227/0337—Heat exchange with the fluid by cooling
    • F17C2227/0339—Heat exchange with the fluid by cooling using the same 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
    • 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
    • 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
    • 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
    • F17C2227/0395—Localisation of heat exchange separate using a submerged heat exchanger
    • 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
    • F17C2250/03—Control means
    • F17C2250/032—Control means using computers
    • 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
    • F17C2250/0621—Volume
    • 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
    • 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
    • F17C2260/00—Purposes of gas storage and gas handling
    • F17C2260/04—Reducing risks and environmental impact
    • F17C2260/046—Enhancing energy recovery
    • 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
    • F17C2265/00—Effects achieved by gas storage or gas handling
    • F17C2265/07—Generating electrical power as side effect
    • 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
    • F17C2270/0118—Offshore
    • F17C2270/0123—Terminals
    • 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
    • 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
    • F17C2270/05—Applications for industrial use
    • F17C2270/0581—Power plants

Definitions

  • the field of the invention is power generation using LNG, and especially as it relates to power generation in LNG regasification facilities, and/or integration to a power plant.
  • Liquefied natural gas (LNG) import is expected to accelerate, mostly due to increased use and technological and economic advantages over crude oil. While some of the currently existing LNG regasification facilities are expanded, new regasification facilities must still be added to meet future demand for natural gas.
  • LNG Liquefied natural gas
  • LNG regasification facilities typically require an external heat source such as an open rack seawater vaporizer, a submerged combustion vaporizer, an intermediate fluid vaporizer (e.g., using a glycol- water mixture), and/or ambient air vaporizers.
  • an external heat source such as an open rack seawater vaporizer, a submerged combustion vaporizer, an intermediate fluid vaporizer (e.g., using a glycol- water mixture), and/or ambient air vaporizers.
  • LNG vaporization is an energy intensive process and typically requires a heat duty equivalent to about 3% of the energy content in LNG. More recently, attempts have been made to reduce the energy requirement for regasification by coupling heat producing processes with the LNG regasification.
  • power plants may be coupled with LNG regasification, as described in
  • heat transfer in some of these configurations is limited by the relatively high freezing point of the heat transfer medium. Due to these and other constraints, power generation efficiency is generally low.
  • power is generated by a steam expansion turbine that is driven by a working fluid (here: water) that is heated by a gas turbine exhaust and cooled by a LNG regasification circuit. While such a configuration increases efficiency of a plant to at least some degree, several problems remain. For example, the utilization of the cryogenic refrigeration content of the LNG is often restricted due to the high freezing point of water.
  • non-aqueous fluids may be employed as a working fluid in a typical Rankine cycle power generation.
  • An exemplary configuration for such approach is disclosed in U.S. Pat. No. 4,388,092 to Matsumoto and Aoki, in which a multi-component hydrocarbon fluid from a distillation column is employed to improve the generation efficiency.
  • operation of these systems and the monitoring and control of the multi- component working fluid is costly and complex.
  • the present invention is directed to configurations and methods for power generation in an LNG regasification operation in which LNG is used as a working fluid, wherein the LNG in liquefied state is used upstream of a vaporizer to condense expanded working fluid, while a portion of the LNG in vaporized state (vaporized natural gas) is used downstream of the vaporizer to drive an expansion turbine.
  • the LNG is vaporized at pipeline pressure, while the condensed expanded working fluid is pumped back to pipeline pressure and combined with the LNG in a position upstream of the vaporizer.
  • an LNG regasification plant that includes a heat exchanger that is configured to condense expanded vaporized natural gas using refrigeration content from liquefied natural gas.
  • a vaporizer in such plants is configured to produce vaporized natural gas from the liquefied natural gas, and an expander is fluidly coupled to the vaporizer and configured to expand at least a portion of the vaporized natural gas to thereby produce the expanded vaporized natural gas.
  • contemplated plants will further include a pump that is configured to receive the condensed natural gas from the heat exchanger and a conduit fluidly coupled to the pump and configured to combine the condensed natural gas with the liquefied natural gas, and/or a second heat exchanger that is configured to heat the at least portion of the vaporized natural gas from the vaporizer using heat from the expanded vaporized natural gas.
  • the plant includes a third heat exchanger that is configured to heat the at least portion of the vaporized natural gas from the vaporizer to a temperature of at least 300 0 F (e.g., using flue gas from a gas turbine, a waste heat recovery unit, and/or a fired heater as a heat source).
  • a heat transfer fluid circuit may be included that is thermally coupled to the vaporizer and a fourth heat exchanger (that is typically configured to heat the portion of the vaporized natural gas from the vaporizer at a position upstream of the expander).
  • Especially contemplated plants will include a second pump that pumps the liquefied natural gas from a storage pressure to a pipeline pressure, wherein the storage pressure is between 1 psig and 100 psig, and wherein the pipeline pressure is between 700 psig and 2000 psig. Therefore, the expander is typically configured to expand the portion of the vaporized natural gas from between about 1000-2000 psig to a pressure of between about 1 psig and 100 psig. It is also contemplated that the plant includes a flow control unit that controls the flow volume of the portion of the vaporized natural gas from the vaporizer to the expander.
  • a method of producing power using natural gas as a working fluid will include a step of expanding at least a portion of vaporized natural gas in a turbine to produce power (typically to a pressure of between 1-100 psig) and expanded vaporized natural gas.
  • the expanded vaporized natural gas is condensed using refrigeration cold of liquefied natural gas, and combining the condensed natural gas with liquefied natural gas, and in yet another step, the combined liquefied and condensed natural gas are vaporized to produce the vaporized natural gas.
  • Especially preferred methods include a step of heating the portion of the vaporized natural gas in one or more heat exchangers using heat from flue gas from a gas turbine, a waste heat recovery unit, a fired heater, and/or the expanded vaporized natural gas. Further preferred methods include a step of pumping the liquefied natural gas to at least pipeline pressure at a location upstream of a vaporizer that produces the vaporized natural gas. Most typically, the vaporizer uses seawater, a heat exchange medium, and/or a submerged burner as a heat source. In preferred aspects of the inventive subject matter, the portion of vaporized natural gas is between about 1% and 50% of the total vaporized natural gas.
  • contemplated open power cycles comprise an expansion turbine and a heater that heats the vaporized natural gas working fluid, while both, the condensed natural gas working fluid and the LNG drawn from the location upstream of the vaporizer are combined and fed to the vaporizer.
  • the LNG at the location upstream of the vaporizer is at about pipeline pressure and the expanded vaporized natural gas working fluid is at a pressure of between 1-100 psig.
  • Figure 1 is one exemplary configuration of a power production scheme coupled to an LNG regasification operation according to the inventive subject matter.
  • Figure 2 is another exemplary configuration of a power production scheme coupled to an LNG regasification operation according to the inventive subject matter.
  • refrigeration content in LNG can be advantageously employed in the production of power in a regasification facility by using at least a portion of the regasified LNG as a working fluid in an open cycle, wherein the LNG is condensed after expansion using the cryogenic refrigeration content of the LNG fed to the facility.
  • an intermediate heat transfer medium may be employed in contemplated configurations.
  • the LNG is pumped to a desired pressure to supply refrigeration in an open power cycle that uses LNG as the working fluid.
  • the LNG working fluid is condensed using the cryogenic temperatures of the LNG that is delivered to the plant. Therefore, it should be recognized that LNG regasification and/or power generation may be accomplished with the use of ambient air vaporizers, seawater vaporizers, and/or waste heat from gas turbine exhaust or fired heaters, which significantly reduces fuel consumption in power generation.
  • no external working fluid is required. Viewed from a different perspective, a substantially increased amount of refrigeration content is recoverable as the working fluid will not freeze at cryogenic temperatures.
  • FIG. 1 An exemplary open LNG power cycle is schematically depicted in Figure 1, in which power generation is operationally coupled to an LNG regasification plant having a send out rate of about 350 MMscfd.
  • inventive subject matter is not limited to a particular send out rate, and suitable plants may have higher or lower rates.
  • Table 1 below shows a typical LNG composition LNG in Figure 1.
  • LNG stream 1 from LNG storage tank or other sources is typically at a pressure between 70 psig to 100 psig and at a temperature of about -260°F to -250 0 F.
  • Stream 1 is pumped by LNG pump 51 to a suitable pressure, typically about 1200 to 1600 psig to form pressurized LNG stream 2, as needed to meet pipeline requirement.
  • a suitable pressure typically about 1200 to 1600 psig to form pressurized LNG stream 2, as needed to meet pipeline requirement.
  • the tenn "about” in conjunction with a numeral refers to a range of that numeral starting from 20% below the numeral to 20% above the numeral, inclusive.
  • the term "about -15O 0 F” refers to a range of -180°F to -120 0 F
  • the term “about 1400 psig” refers to a range of 1372 psig to 1680 psig.
  • a portion of the LNG stream 2 is split off as stream 3 and sent to exchanger 54 using bypass valve 52.
  • Stream 3 is heated in the exchanger from about -250 0 F to about -170 0 F to form stream 4, while the expanded vaporized natural gas working fluid 8 is cooled and condensed from about 40 0 F to about -215°F.
  • the so condensed LNG working fluid 9 is at a pressure of about 80 psig and a temperature of about -215°F and pumped by pump 55 to a pressure of about 1400 psig, forming stream 10 that is combined with the remaining portion of the LNG stream 2 to form combined stream 5.
  • Stream 5 is then heated in vaporizer 53 to about 40 0 F with heat supplied by ambient heat sources (e.g., ambient air or seawater).
  • ambient heat sources e.g., ambient air or seawater
  • the vaporized natural gas stream 6 is then split into a first portion (about 85%, stream 7) and a second portion (about 15%, stream 30) using a flow control device (not shown). It should be noted that, among other factors, the split ratio of the vaporized natural gas stream generally depends on the LNG composition and the desirable power generation output. Stream 7 is sent to the consumer pipeline, while stream 30 is utilized in the power cycle as described below.
  • Stream 30 is first heated in exchanger 56 to about 155°F forming stream 11 using the heat content from the expander discharge stream 13.
  • the so heated vaporized natural gas is further heated in heater 57 with an external source to about 45O 0 F (or higher) forming stream 12.
  • numerous external heat sources are suitable (e.g., flue gas from a gas turbine, waste heat recovery unit, and/or a fired heater).
  • the resultant high pressure high temperature working fluid stream 12 is then expanded in expander 58 to about 75 psig forming stream 13, generating power that can be used to drive an electric generator.
  • Heat content in the expander discharge is recovered in exchanger 56 forming stream 8 that is subsequently condensed in exchanger 54 forming stream 9 to repeat the power cycle.
  • the open power cycle circulates about 550 GPM LNG working fluid, generating about 5,000 kW.
  • the power generation efficiency as calculated by the heat equivalent of net power output from the cycle divided by heat input to exchanger 57, is about 68%.
  • the efficiency can be further increased with higher operating temperature and pressure, which should be balanced with higher equipment costs and heating requirement.
  • stream 30 maybe more than 15% (e.g., 16- 20%, 20-25%, or even higher) of stream 6.
  • stream 3 may vary considerably. Most typically, stream 3 will be at least in an amount effective to condense expanded natural gas stream 8.
  • a first portion of the cryogenic refrigeration content of the LNG stream 2 is used as a heat sink for the LNG working fluid, and that at least a portion of the LNG in at least partially vaporized form is heated and expanded to produce work in an open power cycle.
  • FIG. 2 Another exemplary open LNG power cycle is schematically depicted in Figure 2, in which power generation is operationally coupled to an LNG regasification plant that uses an intermediary heat transfer fluid (e.g., glycol- water, alcohol, or Dowtherm, etc.) to provide heat to the LNG vaporizer.
  • an intermediary heat transfer fluid e.g., glycol- water, alcohol, or Dowtherm, etc.
  • the intermediate fluid stream 14 is pumped by pump 59 to about 120 psig forming stream 15 which is preferably heated with ambient air in vaporizer 60 forming stream 16.
  • a first portion of stream 16 is further heated via stream 17 with waste heat 22 in exchanger 61 to about 480 °F or higher, forming a heated stream 19 that heats the preheated LNG stream 11.
  • Stream 19 exits heat exchanger 57 as stream 20 and is combined with the second portion of stream 16 (stream 18) to form stream 21 that is used in vaporizer 53.
  • stream 19 exits heat exchanger 57 as stream 20 and is combined with the second portion of stream 16 (stream 18) to form stream 21 that is used in vaporizer 53.
  • Suitable heat sources for exchangers 22 and 57 include gas turbine combustion air, cooling water to surface condensers, flue gas from a gas turbine, and/or flue gas from a fuel fired heater.
  • gas turbine combustion air cooling water to surface condensers
  • flue gas from a gas turbine and/or flue gas from a fuel fired heater.
  • suitable recipients for LNG cold may also include numerous cryogenic processes (e.g., air separation plants) in which LNG cools the air or other gas, processes providing flue gas (e.g., reformer flue gases, etc.), and other processes acting as a cold sink (e.g., carbon dioxide liquids production plants, desalination plants, or food freezing facilities).
  • cryogenic processes e.g., air separation plants
  • flue gas e.g., reformer flue gases, etc.
  • cold sink e.g., carbon dioxide liquids production plants, desalination plants, or food freezing facilities.
  • LNG drawn from a location upstream of a vaporizer can be used to condense expanded vaporized natural gas working fluid from a preferably open power cycle wherein the vaporized natural gas working fluid is drawn from a location downstream of the vaporizer.
  • power production is operationally coupled with LNG regasification facilities and/or LNG receiving terminals
  • particularly preferred configurations include those in which LNG is regasified in a process in which at least part of the LNG is used to generate electric power (most preferably with integration to a combined power cycle).
  • suitable plants and methods are described in our commonly owned and co-pending international patent application with the serial numbers PCTYUS03/25372 and PCT/US03/26805, which are incorporated by reference herein. Consequently, and depending on the particular heat source, it should be recognized that the energy needed for regasification of the LNG may be entirely, or only partially provided by contemplated heat sources.
  • supplemental heat may be provided.
  • Suitable supplemental heat sources include waste heat from the steam turbine discharge, condensation duty from the flue gas, ambient heating with air (e.g., by providing air conditioning to buildings), with seawater, or fuel gas. Consequently, it should be appreciated that contemplated configuration and processes may be used to retrofit existing regasification plants to improve power generation efficiencies and flexibility, or may be used in new installations.
  • contemplated configurations provide highly efficient LNG power generation cycles without external working fluid, such as steam, or hydrocarbons with a composition other than LNG.
  • Contemplated processes can be coupled with any type of power plant and still provide benefit or improved efficiency.
  • Especially preferred configurations utilize the LNG cold in the cryogenic region and LNG as the working fluid to achieve high thermal efficiency, typically in the range of about 70% or higher.
  • the LNG send out is pumped to supercritical pressure and regasified using conventional vaporizers while a portion of the regasified product is split off as the LNG working fluid (vaporized natural gas) to the open power cycle.
  • the LNG working fluid is further superheated and expanded to a lower pressure to thereby generate power, wherein the expanded working fluid is condensed utilizing cryogenic temperatures of the LNG send out in the -250°F to -150°F range.
  • the LNG working fluid is pumped to a supercritical pressure (here: above cricondenbar pressure), and heated with an external heat source, and then expanded to a lower pressure for power generation with a heat source integral with or thermally coupled to the power cycle.
  • the expanded working fluid is condensed using the LNG send out, pumped and mixed with the send out LNG and heated in the vaporizers.
  • the power generation according to the inventive subject matter may be implemented as a retrofit to an existing facility or in a facility built from scratch.
  • specific embodiments and applications for configurations and methods for power generation with integrated LNG regasification have been disclosed. It should be apparent, however, to those skilled in the art that many more modifications besides those already described are possible without departing from the inventive concepts herein. The inventive subject matter, therefore, is not to be restricted except in the spirit of the present disclosure.

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  • Engineering & Computer Science (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Filling Or Discharging Of Gas Storage Vessels (AREA)
  • Engine Equipment That Uses Special Cycles (AREA)

Abstract

L'invention porte sur des configurations et méthodes de production d'énergie utilisant le froid de réfrigération du GNL pour condenser du gaz naturel vaporisé expansé produit par une turbine d'expansion entraînée par du gaz naturel vaporisé chauffé extrait d'un vaporiseur. Plus particulièrement le gaz naturel expansé vaporisé combiné au GNL alimente le vaporiseur.
PCT/US2006/027798 2005-07-15 2006-07-17 Configurations et methodes de production d'energie dans des terminaux de regazification de gnl Ceased WO2007011921A2 (fr)

Priority Applications (5)

Application Number Priority Date Filing Date Title
CN200680026102.4A CN101238322B (zh) 2005-07-18 2006-07-17 在液化天然气再气化终端中用于动力生产的结构和方法
EP06787671.4A EP1904782A4 (fr) 2005-07-18 2006-07-17 Configurations et methodes de production d'energie dans des terminaux de regazification de gnl
US11/917,387 US20100030199A1 (en) 2005-07-15 2006-07-17 Configurations And Methods For Power Generation In LNG Regasification Terminals
MX2008000503A MX2008000503A (es) 2005-07-18 2006-07-17 Configuraciones y procedimientos para la generacion de energia en terminales de regasificacion lng.
CA2615850A CA2615850C (fr) 2005-07-18 2006-07-17 Configurations et methodes de production d'energie dans des terminaux de regazification de gnl

Applications Claiming Priority (2)

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US70064905P 2005-07-18 2005-07-18
US60/700,649 2005-07-18

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WO2007011921A3 WO2007011921A3 (fr) 2007-03-08
WO2007011921B1 WO2007011921B1 (fr) 2007-04-19

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EP2159474A1 (fr) * 2008-09-02 2010-03-03 Linde AG Préparation de dioxyde de carbone
WO2011006917A1 (fr) 2009-07-16 2011-01-20 Shell Internationale Research Maatschappij B.V. Procédé et appareil de gazéification de flux d'hydrocarbure liquide
DE102010056585A1 (de) 2010-12-30 2013-06-06 Gea Batignolles Technologies Thermiques Anordnung zur Temperaturerhöhung von flüssigem Erdgas
JP2016503858A (ja) * 2012-12-28 2016-02-08 ゼネラル・エレクトリック・カンパニイ タービンエンジン組立体及び二元燃料航空機システム
KR20190042246A (ko) * 2017-10-16 2019-04-24 두산중공업 주식회사 압력차 발전을 이용한 복합 발전 시스템
EP4101752A4 (fr) * 2020-02-07 2024-03-20 Hanwha Ocean Co., Ltd. Système et procédé de regazéification de gaz liquéfié d'un navire
CN117889349A (zh) * 2024-03-05 2024-04-16 中国科学院工程热物理研究所 一种利用冷能发电的lng气化系统及lng接收站

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EP2609007B1 (fr) * 2010-08-25 2018-04-11 Wärtsilä Gas Solutions Norway AS Procédé et dispositif pour fournir du combustible gnl pour navires
GB2538096A (en) * 2015-05-07 2016-11-09 Highview Entpr Ltd Systems and methods for controlling pressure in a cryogenic energy storage system
SG10201911907RA (en) * 2015-06-29 2020-01-30 Shell Int Research Regasification terminal and a method of operating such a regasification terminal
CN109357159B (zh) * 2018-11-14 2020-11-10 江苏科技大学 一种深冷超临界流体再气化实验系统及工作方法
CN114893268A (zh) * 2022-05-07 2022-08-12 杭州制氧机集团股份有限公司 一种耦合lng冷能利用换冷设备的发电装置及使用方法
WO2025183563A1 (fr) * 2024-02-29 2025-09-04 Wärtsilä Gas Solutions Norway AS Système de regazéification pour gaz liquéfié, navire et procédé de regazéification de gaz liquéfié

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Cited By (10)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP2159474A1 (fr) * 2008-09-02 2010-03-03 Linde AG Préparation de dioxyde de carbone
WO2011006917A1 (fr) 2009-07-16 2011-01-20 Shell Internationale Research Maatschappij B.V. Procédé et appareil de gazéification de flux d'hydrocarbure liquide
DE102010056585A1 (de) 2010-12-30 2013-06-06 Gea Batignolles Technologies Thermiques Anordnung zur Temperaturerhöhung von flüssigem Erdgas
JP2016503858A (ja) * 2012-12-28 2016-02-08 ゼネラル・エレクトリック・カンパニイ タービンエンジン組立体及び二元燃料航空機システム
US9765691B2 (en) 2012-12-28 2017-09-19 General Electric Company Turbine engine assembly and dual fuel aircraft system
KR20190042246A (ko) * 2017-10-16 2019-04-24 두산중공업 주식회사 압력차 발전을 이용한 복합 발전 시스템
KR102023003B1 (ko) * 2017-10-16 2019-11-04 두산중공업 주식회사 압력차 발전을 이용한 복합 발전 시스템
US10968826B2 (en) 2017-10-16 2021-04-06 DOOSAN Heavy Industries Construction Co., LTD Combined power generation system using pressure difference
EP4101752A4 (fr) * 2020-02-07 2024-03-20 Hanwha Ocean Co., Ltd. Système et procédé de regazéification de gaz liquéfié d'un navire
CN117889349A (zh) * 2024-03-05 2024-04-16 中国科学院工程热物理研究所 一种利用冷能发电的lng气化系统及lng接收站

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CN101238322A (zh) 2008-08-06
EP1904782A2 (fr) 2008-04-02
CA2615850C (fr) 2011-01-25
MX2008000503A (es) 2008-03-07
WO2007011921A3 (fr) 2007-03-08
EP1904782A4 (fr) 2015-01-14
WO2007011921B1 (fr) 2007-04-19
CN101238322B (zh) 2012-11-14
CA2615850A1 (fr) 2007-01-25

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