EP3320257B1 - Procédé de regazéification de gaz naturel liquéfié - Google Patents

Procédé de regazéification de gaz naturel liquéfié Download PDF

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EP3320257B1
EP3320257B1 EP16759684.0A EP16759684A EP3320257B1 EP 3320257 B1 EP3320257 B1 EP 3320257B1 EP 16759684 A EP16759684 A EP 16759684A EP 3320257 B1 EP3320257 B1 EP 3320257B1
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gas
temperature
pressure
vaporizer
lng
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EP3320257A1 (fr
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Rafal Chmielewski
Marek GOSCICKI
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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
    • F17C5/00—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures
    • F17C5/06—Methods or apparatus for filling containers with liquefied, solidified, or compressed gases under pressures for filling with compressed gases
    • 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
    • F17C2225/0115—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
    • 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
    • F17C2225/035—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
    • 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
    • F17C2227/0327—Heat exchange with the fluid by heating with recovery of heat
    • 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
    • F17C2227/0332—Heat exchange with the fluid by heating by burning a combustible
    • 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
    • F17C2227/0369—Localisation of heat exchange in or on a vessel
    • 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
    • F17C2227/04—Methods for emptying or filling
    • F17C2227/047—Methods for emptying or filling by repeating a process cycle
    • 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
    • F17C2250/01—Intermediate tanks
    • 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

Definitions

  • the present invention relates to a method for regasifying liquefied natural gas as and a system for regasifying liquefied natural gas.
  • natural gas typically contains about 80 - 98 vol % of methane and, after condensation, its volume is reduced 600 times, which makes it economically feasible for transport.
  • Liquefied natural gas (LNG) is transported at atmospheric pressure, in the temperature of about -160 °C, i.e. below the critical gas temperature (which is -82,5 °C for pure methane). It is known that above the critical gas temperature, the methane can be in a gaseous phase only, regardless of the pressure conditions. LNG may be transported by sea, for example by tank ships called LNG carriers.
  • the liquefied gas is transferred to ground LNG storage tanks which are also called LNG-receiving terminal tanks.
  • ground LNG storage tanks which are also called LNG-receiving terminal tanks.
  • the liquefied gas is transferred to a regasification plant to convert the LNG to the gaseous state.
  • the main components of the regasification are vaporizers that convert the LNG to the gaseous state.
  • vaporizers that may have different construction, conversion efficiency and way of heating of the natural gas.
  • the type of the vaporizer is selected due to the location of the LNG regasification plant and due to the accessibility of the heating medium.
  • vaporizers supplied with sea water operate as spry coolers consisting of suitably ribbed pipes or plates with wavy profile.
  • the LNG flows through the pipes or through the slits between two adjacent plates, wherein the heating medium in the form of a thin water layer heats the gas flowing in countercurrent, on the outer surface of the pipes or plates.
  • the vaporizers of this type provide efficient heat exchange between the heating medium and the LNG and have a relatively high regasification yield.
  • the construction of the vaporizers provides indirect heat exchange between the heating medium and the gas.
  • air-heated vaporizers have the form of multi-sectional heat exchangers, wherein the LNG flows as a gas stream through the pipes, and the air (as the heating medium) flows as a stream within the inter-pipe space.
  • the heating is conducted both directly (by the air which cools down when it transmits the heat) and indirectly (by introducing the hot air).
  • the exhausted heating medium i.e. the "cold” that constitutes the byproduct of the LNG regasification
  • the exhausted heating medium is typically used as a cooling medium for various technological processes, for example to produce oxygen and nitrogen by distillation of liquefied air or to separate hydrocarbon gases in a petrochemical or refining industry.
  • a European patent application EP1634023 discloses a method for regasifying LNG, comprising splitting a liquid natural gas feed into a first portion and a second portion; using a refrigeration content of the first portion to cool a heat source in the plant and thereby generating a heated first portion; expanding the heated first portion as a working fluid to produce electric power and an expander outlet stream; feeding the expander outlet stream into a demethanizer; and using the second portion as reflux for the demethanizer.
  • a PCT application WO2012102849 discloses a method for regasifying LNG, comprising: providing heat to a LNG regasification process from a power plant; and, if the heat is not sufficient, providing additional heat to the LNG regasification process from a cooling tower operated in a warming tower configuration.
  • the "cold" obtained in the regasification process is used to cooling down the exhaust gases of the gas turbine.
  • US5237824A relates to a process and apparatus for delivering supercritical fluid.
  • the known LNG regasification systems enable LNG to be converted back to the gaseous state by using various heat sources.
  • the "cold" constituting the byproduct of the regasification process is used in the low temperature processes, which provides the reduction of total energy consumption in the regasification process.
  • Fig. 1 shows schematically a block diagram of a system and a method for regasifying liquefied natural gas (LNG) i.e. for conversion of the LNG back to the gaseous state having particular parameters (preferably, corresponding to legal regulatory provisions) that enable the gas to be transported in the gaseous state via gas pipelines.
  • the LNG may be introduced to the regasification system from an LNG storage tank 101 by means of a thermally insulated pipeline provided with a pump system configured to pump the LNG.
  • the regasification system comprises a system of high-pressure vaporizers 102 for conversion of the LNG back to the gaseous state.
  • the number of the vaporizers in the system 102 may depend on the processing capacity of the regasification system and on the pressure stability that is required within the system.
  • the vaporizers system 102 can comprise one high-pressure vaporizer, two high-pressure vaporizers, three high-pressure vaporizers or more than three high-pressure vaporizers.
  • the LNG is periodically introduced (in batches) to the vaporizers system 102.
  • the mass (volume) of one LNG batch should correspond to the processing capacity of the vaporizers 102.
  • the LNG is regasified in a multiphase process.
  • the LNG is converted to the gaseous state by increasing the LNG temperature from a first temperature T 1 (which is -160°C) to a second temperature T 2 (which is equal the critical temperature of natural gas).
  • the critical temperature of natural gas may vary depending on the chemical composition of the natural gas. For example, the critical temperature of pure methane is -82,5°C, and the critical temperature of a gas composition contaminated with ethane can be higher (such as -48°C).
  • the temperature of the gas increased form the critical temperature of the gas composition (T 2 ) to the third gas temperature (T 3 ), such as +10°C.
  • the pressure of the gas in the vaporizer increases form a first pressure p 1 corresponding to the residual gas pressure in the system (which is about 0,1 MPa), to a final pressure p 2 which can be at least 7MPa, and more preferably at least 10MPa, or at least 20MPa, or at least 50MPa, or at least 70MPa, or at least 100MPa.
  • the higher the final pressure p 2 the better the final efficiency of the regasification process. It is possible to obtain such a high pressure (without additional compression of the gas) when the chamber of the high-pressure vaporizer is filled as much as possible with the LNG.
  • 85% to 99% of the volume of the chamber 204 of the high-pressure vaporizer should be filled with the LNG.
  • heat in the form of a heating medium is introduced to the vaporizers system 102 in two phases.
  • first phase of the regasification process when the temperature is increased form the first temperature T 1 to the second temperature T 2 , lower quality heat is used as the heating medium, preferably in the form of a fluid having a temperature that is higher than the critical gas temperature, preferably having a temperature equal to the ambient temperature.
  • the lower quality heat medium may have a temperature between -30°C and +50°C.
  • the lower quality heat can be: heat constituting a byproduct produced by the cooling system of a frozen food warehouse, or heat from the environment in winter (the difference between the temperature of LNG and the circulating medium is low), or heat constituting a byproduct of the following processes: freeze-drying, recycling or heat form environment.
  • the gas is heated form the second temperature T 2 to the third gas temperature T 3 , which can be equal to the ambient temperature.
  • higher quality heat is introduced to the vaporizers system 102.
  • the higher quality heat constitutes the heating medium, preferably in the form of a fluid of the temperature that is higher than the temperature of the lower quality heating medium.
  • the temperature of the higher quality heating medium is higher than the ambient temperature.
  • the temperature of the higher quality heating medium is between 50°C and 250°C.
  • Liquids or gases can be used as the higher quality heating medium, such as a byproduct of a freeze-drying process, or a steam produced in the process of re-sublimation or heat obtained in the process of combustion of biomass.
  • the gas After the gas reaches the third temperature T 3 and the final pressure p 2 , the gas is to be decompressed in order to recover the mechanical energy, which can be used for example to power an electric generator.
  • the heat that is necessary to carry out the regasification process may be supplied to the vaporizers system 102 in various ways.
  • the heat exchange system of the vaporizers 102 may be provided with a system of ventilators that enable the introduction of the air into the heat exchange system.
  • the air exhausted in the heat exchange process (which is cooled, deprived of moisture and dried) may be used in various low-temperature processes, for example, the air may be used for drying biomass, which improves the combustion efficiency (yield) of the drying process and enables reduction of water content in the biomass, which further provides higher combustion temperature.
  • Fig. 2 shows schematically a vaporizer 102 for use in the regasification system.
  • the thermally insulated high-pressure vaporizer 102 comprises an inlet 201, by which the LNG having a first temperature T 1 and a pressure of about 0,1MPa is periodically introduced, in batches, to a first chamber 202 of the vaporizer. From the first chamber, the LNG flows by gravity into a second chamber 204 of the vaporizer by a passage 203.
  • the second chamber 204 is provided with a heat exchange system 205, for example in the form of cooling coil with the heating medium in the form of a liquid or a gas flowing through the coil.
  • the passage 203 is closed, and the LNG collected in the second chamber 204 is converted back to the gaseous state by means of increasing the LNG temperature form the first temperature T 1 to the second temperature T2, and next, increasing the natural gas temperature to the third temperature T 3 (for example, to 200°C).
  • the pressure of the natural gas in the second chamber 204 of the vaporizer increases from the first pressure p 1 to the second pressure p 2 .
  • the natural gas is decompressed in order to fill, in a gaseous form, the storage tank 103 (which can be also called an expansion tank).
  • the gas In order to decompress the gas collected in the second chamber 204 of the vaporizer, the gas is released form the second chamber 204 by opening the outlet 206 of the second chamber 204, which is connected by pipes with a storage storage tank 103. Due to the pressure difference between the vaporizer chamber (p 2 ) and the chamber of the storage tank 103 (lower than p 2 ), the gas flows towards the lower pressure tank providing spontaneous collection of the gas within the storage tank 103 chamber. Such construction reduces the energy expenditure associated with the transfer of the gas form the vaporizer 102 to the storage tank 103. Moreover, the storage storage tank 103 provides reduction of pressure fluctuations within the regasification system.
  • the flow of the gas between the vaporizer 102 and the storage tank 103 is blocked by closing the outlet 206 of the vaporizer, which enables to introduce into the second chamber 204 of the vaporizer a next batch of the LNG to be regasified. Additionally, in order to reduce the pressure in the chamber 204 of the vaporizer to the pressure which equals the pressure of the LNG chamber 101, the gas that remains in the vaporizer chamber 204 may be pumped out of the chamber 204 to the gas pipeline.
  • the expansion of gas is an endothermic process, which causes reduction of the temperature of the decompressed gas form the third temperature T 3 to a fourth temperature T 4 that is lower than the third temperature T 3 .
  • the fourth temperature T 4 of the gas after its expansion may be different depending on the initial gas parameters, i.e. the parameters of the gas before the expansion.
  • the fourth temperature T 4 may be, for example, form -50°C to 0°C.
  • the gas form the storage tank 103 is introduced to the energy conversion cell 105 and the gas is heated form the fourth temperature T 4 to the fifth temperature T 5 , which may be from +10 to +250°C by means of a heat exchange system 110, which is connected to the storage tank 103 and supplied with the higher quality heat having parameters as discussed above.
  • a heat exchange system 110 which is connected to the storage tank 103 and supplied with the higher quality heat having parameters as discussed above.
  • heat produced by the biomass combustion system 105 co-operating with the regasification system can be used as the higher quality heat.
  • the biomass combustion system can be provided with a drying station 109. Heating of the gas before its introduction into the energy conversion cell 105 causes rise of the gas pressure.
  • the gas pressure rises to the level from 10 MPa to 100 MPa.
  • the gas that is heated in the storage tank is introduced into the energy converter of the energy conversion cell 105.
  • the gas is decompressed to the pressure which is higher than the pressure of the gas in the gas pipeline 108.
  • the gas cooled in the energy conversion cell 105 by means of decompression, is introduced to a system of heat exchangers 106, 107 enabling the gas to be heated to the required temperature.
  • the first heat exchanger 106 is supplied with air and it enables pre-heating of the gas.
  • the second heat exchanger 107 is supplied with the heat form the biomass combustion process 104 and it enables heating of the gas, preferably to the temperature of +10°C.
  • the "cold" that is collected by the heating medium of the heat exchangers 106, 107 is used in the installations co-operating with the regasification system, wherein cooled and dried air leaving the first heat exchanger 106 is used for drying the biomass in the biomass drying station 109, and the cooled heating medium leaving the second heat exchanger 107 is used as the heat exchanging medium in the medium-temperature system 111 co-operating with the regasification system, which may be, for example, systems for production frozen food or freeze-dried products.
  • the regasification system enables collection of the "cold" at each phase of the process, by means of the system of heat exchangers in which liquid or gas may be use as the heating medium, which depends on the construction of the heat exchangers co-operating with the vaporizers system 205, the storage tank 110 and the first and second heat exchanger 106, 107 for heating the gas before its enters the gas pipeline.
  • the "cold” that is produced during the liquid-to-gas conversion process as well as during gas expansion, constitutes the byproduct of the regasification process and it is supplied to the various process where it is used - this provides a suitable way of reprocessing of the produced "cold" in an environment friendly manner.
  • the regasification system may additionally comprise a system of conventional vaporizers 112 having a variable volume, which can operate in the conditions of residual pressure in the system of about 0,1MPa, and which can receive the "cold" used in the low-temperature system 114, such as for example in the processes of oxygen and nitrogen production by air rectification.
  • the vaporizers there may be used conventional continuous operation mode vaporizers with an air heat exchange system.
  • the gas of a substantially low pressure (0,1MPa or so) after regasification, may be transferred into a gas tank 113, and subsequently the gas may be compressed to the required pressure by heating the gas, and then the gas can be transferred to the storage tank 103.
  • the "cold” produced in the regasification batch process may be used in the process of production of frozen food, freeze-dried food products for humans or animals, in some stages of drugs production as well as in the process of production organic products.
  • the "cold” produced in the regasification process may be additionally used in the processes of recycling of low-temperature polymers and plastics, such as for example, low-temperature depolymerization or shredding or in the warehouses or cold rooms for cooling.
  • the “cold” may be also used in the processes of electricity generation or in the processes of production of mechanical energy in a "mono” process: from the cold with the potential of environment as the main heat source, or in a “dual” process with the potential of combustion of the ecological fuels as the main heat source.
  • the "cold” produced in the regasification system may be also used to produce ice-water for buildings, hotels, malls, spa centers and large volume laboratories for testing machinery and vehicles in low temperatures, or for research processes related to roads and bridges.
  • the "cold” may be also used in sports facilities such as, for example ice rinks or snow-covered terrains for skiing which are located near the regasification system.
  • the "cold” may be used in the low-temperature technology centers that carry out research on the use of the low temperatures in biology or physics, such as for example to conduct research on Peltier's and Seebeck's superconductivity phenomena.
  • the heat required to raise the temperature of natural gas either in the liquid or in the gaseous state is derived from various processes, co-operating with the regasification system, in which the heat constitutes byproduct, such as for example the processes of freeze-drying or recycling processes.
  • the regasification system is also additionally supplied with heat from biomass combustion, wherein the dried air that constitutes the exhausted heating medium, after the gas heating process carried out in the heat exchanger, is used for drying the biomass.
  • biomass combustion reduce heat absorption form the environment, for example from water, which further reduces possible local temperature decreases which could be dangerous for the local biocoenosis.
  • high-pressure vaporizers in the regasification system provides improves the energy efficiency of the whole regasification system.
  • Reaching of high gas pressure (such as at least 7MPa, or more preferably at least 10MPa, or at least of 20MPa, or at least 50MPa, or at least 70MPa, or at least 100MPa) provides spontaneous transfer of the gas to the storage tank - without the necessity of using additional equipment such as force pumps which require additional power supply.
  • the maintenance of the gas at the high pressure, such as of about 100MPa, in the storage tank provides further spontaneous transfer of the gas from the storage tank to the energy conversion cell and to the gas pipeline according to the pressure gradient - without the necessity of using additional equipment such as force pumps; the gas enters the gas pipeline due to its own pressure.
  • the construction of the regasification system as well as the implementation of the vaporizers system reduces the necessity of using additional pumps to transfer natural gas between the respective elements of the regasification system, which further provides the reduction of energy consumption and emission od CO 2 of the regasification system.
  • the two-phase regasification process in the vaporizer in which at the first phase the liquid-to-gas conversion is carried out by means of heating LNG to its critical temperature by the heat of lower quality, and at the second phase the gas in the gaseous state is heated, by means of heat of higher quality, to the temperature that provides the optimal rise of gas pressure in the regasification process, additionally improves the energy efficiency (energy saving) in the regasification process.

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

Claims (8)

  1. Procédé permettant la regazéification de gaz naturel liquéfié (GNL), comprenant les étapes de :
    - entrée d'un lot de gaz naturel liquéfié dans une chambre (204) d'un vaporisateur (102), la pression du gaz correspondant à la pression résiduelle dans le système d'environ 0,1 MPa ;
    - dans le vaporisateur (102), la conversion du gaz naturel liquéfié à l'état gazeux en le chauffant au moyen d'un fluide chauffant de qualité inférieure d'une première température (T1) à une deuxième température (T2) qui est une température critique de la composition gazeuse et le chauffage du gaz au moyen d'un fluide chauffant de qualité supérieure de la deuxième température (T2) à une troisième température (T3) supérieure à la température critique du gaz pour augmenter la pression du gaz jusqu'à une seconde pression (p2) supérieure ou égale à 7 MPa, ledit milieu chauffant de qualité inférieure comportant une température inférieure à celle du milieu chauffant de qualité supérieure ;
    - le raccordement de la sortie de gaz du vaporisateur (102) à un réservoir de stockage (103) comportant une chambre avec une pression inférieure à la pression du vaporisateur (102) ; et
    - l'autorisation au gaz provenant du vaporisateur (102) de s'écouler et de se dilater dans le réservoir de stockage (103) en raison de la différence de pression entre le vaporisateur (102) et le réservoir de stockage (103).
  2. Procédé selon la revendication 1, ledit lot de gaz naturel liquéfié remplissant de 85 % à 99 % du volume de la chambre (204) du vaporisateur (102).
  3. Procédé selon l'une quelconque des revendications précédentes, comprenant en outre l'augmentation de la température du gaz dans le réservoir de stockage (103) jusqu'à la plage allant de +10°C à +250°C.
  4. Procédé selon la revendication 3, comprenant en outre le transfert du gaz du réservoir de stockage (103) à une cellule de conversion d'énergie (105) comprenant un convertisseur d'énergie ; et l'autorisation au gaz de se dilater et la conversion de l'énergie de dilatation du gaz en énergie électrique.
  5. Procédé selon la revendication 1, ledit milieu chauffant de qualité inférieure étant un sous-produit d'un processus de congélation, de lyophilisation ou de recyclage.
  6. Procédé selon la revendication 1, ledit milieu chauffant de qualité supérieure étant un sous-produit d'un processus de lyophilisation ou de combustion de biomasse.
  7. Procédé selon la revendication 4, comprenant en outre le chauffage du gaz détendu dans la cellule de conversion d'énergie (105) dans un système d'échange de chaleur (106, 107) et l'introduction du gaz dans un gazoduc (108).
  8. Procédé selon la revendication 7, comprenant le chauffage du gaz détendu dans la cellule de conversion d'énergie (105) dans un premier échangeur de chaleur (106) par de l'air et un chauffage ultérieur dans un second échangeur de chaleur (107) par de la chaleur constituant un produit du processus de combustion de biomasse.
EP16759684.0A 2015-07-06 2016-07-05 Procédé de regazéification de gaz naturel liquéfié Active EP3320257B1 (fr)

Applications Claiming Priority (2)

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PL413001A PL413001A1 (pl) 2015-07-06 2015-07-06 Sposób regazyfikacji skroplonego gazu ziemnego oraz system regazyfikacji skroplonego gazu ziemnego
PCT/EP2016/065750 WO2017005708A1 (fr) 2015-07-06 2016-07-05 Procédé de regazéification de gaz naturel liquéfié, et système de regazéification de gaz naturel liquéfié

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Citations (2)

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US5237824A (en) * 1989-02-16 1993-08-24 Pawliszyn Janusz B Apparatus and method for delivering supercritical fluid
US20130327421A1 (en) * 2010-11-30 2013-12-12 Korea Advanced Institute Of Science And Technology Apparatus for Pressurizing Delivery of Low-Temperature Liquefied Material

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Publication number Priority date Publication date Assignee Title
US5243821A (en) * 1991-06-24 1993-09-14 Air Products And Chemicals, Inc. Method and apparatus for delivering a continuous quantity of gas over a wide range of flow rates
WO2004109206A1 (fr) * 2003-06-05 2004-12-16 Fluor Corporation Configuration et procede de regaseification de gaz naturel liquefie
MX2007003102A (es) * 2004-09-22 2007-05-16 Fluor Tech Corp Configuraciones y metodos para gas licuado de petroleo y co-generacion de energia.
SG191195A1 (en) 2011-01-28 2013-07-31 Exxonmobil Upstream Res Co Regasification plant
BR112014010651B1 (pt) * 2011-11-02 2021-02-09 8 Rivers Capital, Llc sistema de geração de energia e método correspondente

Patent Citations (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US5237824A (en) * 1989-02-16 1993-08-24 Pawliszyn Janusz B Apparatus and method for delivering supercritical fluid
US20130327421A1 (en) * 2010-11-30 2013-12-12 Korea Advanced Institute Of Science And Technology Apparatus for Pressurizing Delivery of Low-Temperature Liquefied Material

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