EP2724100B1 - Procédé de liquéfaction de gaz naturel a triple circuit ferme de gaz réfrigérant - Google Patents

Procédé de liquéfaction de gaz naturel a triple circuit ferme de gaz réfrigérant Download PDF

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Publication number: EP2724100B1
Authority: EP; European Patent Office
Prior art keywords: compressor; flow; gas; exchanger; pressure
Prior art date: 2011-06-24
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.): Active

Application number

EP12731601.6A

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German (de)

English (en)

French (fr)

Other versions

EP2724100A2 (fr

Inventor

Marc Bonnissel

Bertrand DU PARC

Eric ZIELINSKI

Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)

Saipem SpA

Original Assignee

Saipem SpA

Priority date (The priority date 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 date listed.)

2011-06-24

Filing date

2012-06-22

Publication date

2020-12-02

2012-06-22 Application filed by Saipem SpA filed Critical Saipem SpA

2012-06-22 Priority to SI201231880T priority Critical patent/SI2724100T1/sl

2012-06-22 Priority to HRP20210341TT priority patent/HRP20210341T1/hr

2012-06-22 Priority to RS20210238A priority patent/RS61507B1/sr

2014-04-30 Publication of EP2724100A2 publication Critical patent/EP2724100A2/fr

2020-12-02 Application granted granted Critical

2020-12-02 Publication of EP2724100B1 publication Critical patent/EP2724100B1/fr

Status Active legal-status Critical Current

2032-06-22 Anticipated expiration legal-status Critical

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- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
- F25J1/0022—Hydrocarbons, e.g. natural gas
- F25J1/0025—Boil-off gases "BOG" from storages
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
- F25J1/0047—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle
- F25J1/005—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using an "external" refrigerant stream in a closed vapor compression cycle by expansion of a gaseous refrigerant stream with extraction of work
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/007—Primary atmospheric gases, mixtures thereof
- F25J1/0072—Nitrogen
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/006—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the refrigerant fluid used
- F25J1/0097—Others, e.g. F-, Cl-, HF-, HClF-, HCl-hydrocarbons etc. or mixtures thereof
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0203—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle
- F25J1/0204—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a single-component refrigerant [SCR] fluid in a closed vapor compression cycle as a single flow SCR cycle
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
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- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0211—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle
- F25J1/0212—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using a multi-component refrigerant [MCR] fluid in a closed vapor compression cycle as a single flow MCR cycle
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0244—Operation; Control and regulation; Instrumentation
- F25J1/0254—Operation; Control and regulation; Instrumentation controlling particular process parameter, e.g. pressure, temperature
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0283—Gas turbine as the prime mechanical driver
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0281—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc. characterised by the type of prime driver, e.g. hot gas expander
- F25J1/0284—Electrical motor as the prime mechanical driver
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0287—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings including an electrical motor
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0285—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings
- F25J1/0288—Combination of different types of drivers mechanically coupled to the same refrigerant compressor, possibly split on multiple compressor casings using work extraction by mechanical coupling of compression and expansion of the refrigerant, so-called companders
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
- F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
- F25J1/0243—Start-up or control of the process; Details of the apparatus used; Details of the refrigerant compression system used
- F25J1/0279—Compression of refrigerant or internal recycle fluid, e.g. kind of compressor, accumulator, suction drum etc.
- F25J1/0289—Use of different types of prime drivers of at least two refrigerant compressors in a cascade refrigeration system
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/20—Integrated compressor and process expander; Gear box arrangement; Multiple compressors on a common shaft
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
- F25J2230/22—Compressor driver arrangement, e.g. power supply by motor, gas or steam turbine
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
- F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion loop
- F25J2270/16—External refrigeration with work-producing gas expansion loop with mutliple gas expansion loops of the same refrigerant

Definitions

the present invention relates to a process for liquefying natural gas to produce LNG, or Liquefied Natural Gas, also called LNG. More particularly still, the present invention relates to the liquefaction of natural gas mainly comprising methane, preferably at least 85% of methane, the other main constituents being chosen from nitrogen and C-2 to C-4 alkanes. namely ethane, propane, butane.
the present invention also relates to a liquefaction installation arranged on a ship or a floating support at sea, either in the open sea or in a protected area, such as a port, or even an onshore installation in the case of small or medium-sized vessels. liquefaction of natural gas.
the present invention relates more particularly to a process for re-liquefying gas on board an LNG transport ship called a “methane tanker”, said gas to be re-liquefied being the result of reheating and partial evaporation of the LNG contained in the tanks of said vessel, said evaporated gas, in general mainly methane, being called in English “boil off”.
Methane-based natural gas is either a by-product of oil fields, produced in small or medium quantities, usually associated with crude oil, or a major product in the case of gas fields, where it is then in combination with other gases, mainly C-2 to C-4 alkanes, CO2, nitrogen.
cryogenic liquid -165 ° C
LNG carriers Specialized transport vessels have very large tanks with extreme insulation so as to limit evaporation during the voyage.
the liquefaction of gas for transport is generally carried out near the production site, generally on land, and requires considerable facilities to reach capacities of several million tonnes per year, the largest existing units grouping together three or four liquefaction units of 3-4 Mt per year of unit capacity.
This liquefaction process requires considerable amounts of mechanical energy, the mechanical energy being generally produced on site by taking part of the gas to produce the energy necessary for the liquefaction process. Part of the gas is then used as fuel in gas turbines, steam turbines or reciprocating heat engines.
thermodynamic cycles have been developed in order to optimize the overall energy efficiency.
a first type based on the compression and expansion of refrigerant fluid, with phase change
a second type based on the compression and expansion of refrigerant gas without phase change.
refrigerant fluid or “refrigerant gas” is used to refer to a gas or mixture of gases, circulating in a closed circuit and undergoing compression phases, where appropriate liquefaction, then heat exchanges with the external environment, then subsequently phases of expansion, where appropriate of evaporation, and finally of heat exchanges with the natural gas to be liquefied comprising methane, which gradually cools down to reach its liquefaction temperature at atmospheric pressure, i.e. approximately - 165 ° C in the case of LNG.
Said first type of cycle, with phase change, is in general used on land installations and requires a large amount of equipment and a considerable footprint.
refrigerant fluids generally in the form of mixtures, consist of butane, propane, ethane and methane, these gases being dangerous because they risk, in the event of leakage, causing explosions or considerable fires. .
they remain the most efficient and require energy of the order of 0.3 kWh per kg of LNG produced.
the second type of liquefaction process a process without phase change of the refrigerant gas
the efficiency of this second type is lower, because it generally requires an energy of the order of 0.5 kWh / kg of LNG produced, i.e. about 20.84 kW x day / t and, on the other hand, it has a considerable advantage in terms of safety, because the refrigerant gas of the cycle, nitrogen, is inert and therefore incombustible, which is very interesting when the installations are concentrated in a small space, for example on the deck of a floating support installed in the open sea, said equipment often being installed on several levels, one above the other on a small surface to the bare minimum.
a refrigerant gas leak there is no danger of explosion and it is then sufficient to reinject the lost refrigerant gas fraction into the circuit.
this method of liquefying natural gas without phase change is very advantageous in the case of floating supports, because, due to the absence of a liquid phase in the refrigerant gas, the equipment is of much simpler design. In fact, in such installations, all of the equipment moves almost continuously to the rhythm of the movements of the floating support (roll, pitch, yaw, sheer, swing, heave). And the management of a process with phase change involving a liquid phase of the refrigerant would be extremely delicate even for weak movements of the floating support, or even almost impossible for extreme movements, whereas in fixed installations on land the problem of movements does not arise.
the refrigerant in the case of the phase change cycle of the refrigerant fluid, for the yields to remain optimum, the refrigerant must be adapted to the nature and composition of the gas to be liquefied. and the composition of the refrigerant fluid must, if necessary, be modified over time, depending on the composition of the mixture of natural gas to be liquefied produced by the oil field.
the refrigerant gas remains in the gaseous state and circulates continuously as explained previously: it gradually gives up frigories, therefore gradually absorbs calories from the gas to be liquefied, namely a mixture consisting mainly of of methane and other traces of gas.
the circulation of the gas to be liquefied takes place against the current of the refrigerant gas, that is to say that said natural gas comprising methane enters substantially at ambient temperature into the exchanger at the level of the refrigerant gas outlet where the latter is then substantially at room temperature.
said natural gas comprising methane progresses through the exchanger towards the colder zones and transfers its calories to the refrigerant fluid: the natural gas comprising methane cools and the refrigerant gas heats up.
T3 -165 ° C for a gas containing 85% methane.
Phase 2 consumes the most energy, because the gas must be supplied with all the energy corresponding to its latent heat of vaporization. Phase 1 consumes a little less energy, and phase 3 consumes the least energy, on the other hand it is done at the lowest temperatures, i.e. around -165 ° C.
T1, T2 and T3 are suitable for a natural gas consisting of 85% methane and 15% of said other components nitrogen and C-2 to C-4 alkanes, and can vary significantly for a gas of different composition.
FIG. 1 there is shown an installation diagram of a standard natural gas liquefaction process involving a refrigerant gas consisting of nitrogen without phase change of the refrigerant gas as described above and the description of the process of which is explained later. .
the pressure levels P1 and P2 of the gases leaving the turbines 112 and 111 are different and therefore the flow rates passing through the regulators 111 and 112 are different and in particular in practice in a ratio of 10-20% of the total flow for the flow rate of the flow from expander 112 against 80-90% for the flow rate from expander 111.
compressor 115b only recovers 10-20% of the total power recovered compared to 80-90% of power recovered at the level compressor 115a.
This disparity in power supplied to the two compressors 115a and 115b mounted in parallel results in a major difficulty in stabilizing the operation of the circuit.
Stabilization of the operation of the circuit can be carried out conventionally by means of control valves upstream and / or downstream of said compressors 115a and 115b mounted in parallel, and / or upstream and / or downstream of said turbines 111 and 112 to control the compressors flow rates and operation.
control valves upstream and / or downstream of said compressors 115a and 115b mounted in parallel, and / or upstream and / or downstream of said turbines 111 and 112 to control the compressors flow rates and operation.
these control valves generate pressure losses, and therefore energy, which affects greatly the desired overall efficiency and / or the production capacity of the installation.
the aim of the present invention is to provide a process for the liquefaction of natural gas of the type without phase change of the refrigerant gas capable of being installed on a ship or floating support which has improved energy efficiency, namely a total energy consumed in the tank. minimum process in terms of kWh to obtain 1 tonne of LNG and / or which exhibits increased heat transfers in the exchangers and / or which makes it possible to implement a more compact and efficient liquefaction installation.
the term “compressor coupled to an expansion valve / turbine or engine” or “compressor actuated by an engine” (or vice versa a “expansion valve / turbine or engine coupled to the compressor”) is understood to mean that the output shaft of the turbine or respectively of the engine drives the input shaft of the compressor, that is to say, transfers mechanical energy to the shaft of the compressor. It is therefore a mechanical coupling of the compressor to the expansion valve / turbine or respectively of the compressor to the engine.
said motor can be either a heat engine, or preferably an electric motor, or any other installation capable of supplying mechanical energy to the refrigerant gas; and the compressors are of the rotary turbine type, also called a centrifugal compressor.
step (a) the liquefied natural gas leaving said third exchanger is depressurized at T3, from pressure P0 to atmospheric pressure where appropriate.
the method according to the invention is advantageous over the method described in US 2011/0113825 in that all the compressors are mounted in series without requiring flow control with flow control valves to stabilize the operation of the installation. In fact, in the process according to the invention, there is no separation of flows in the compression chain. It follows that the regulation of flow rate of flow and / or energy at the level of the various compressors is obtained essentially by the regulation of the power input at the level of said first and second engines and said gas turbine. It is not essential to implement control valves at said compressors and said turbine because said first and second expansion valves are coupled to said first and second compressors mounted in series and are therefore not coupled to compressors mounted in series. parallels as in US 2011/0113825 .
first and second compressors in series coupled to said first and second expansion valves also makes it possible to improve the compactness of the installation, which is particularly advantageous for the implementation of a process. aboard a floating support where space is limited.
the method according to the invention with reference to figures 2- 3 is advantageous over that of figure 1 in that, first of all, rather than recycling after expansion a part D2 of the second flow at the outlet of the first exchanger to join the first flow at the inlet of the second exchanger, this part D2 is recycled from the second flow to the entry of the second exchanger at an intermediate pressure P2 greater than P1 in a third independent flow S3 and parallel to S1, that is to say in co-current of S1. And, because most of the energy is consumed for phase 2 of the process within said second exchanger, this makes it possible to increase the heat transfers and the energy efficiency of the process.
the method according to the invention is advantageous over WO 2005/071333 and the method described in the GASTECH 2009 review cited above in that it allows said pressure P2 to be varied in a controlled manner so that the energy consumed for implementing the method (Ef) is minimal.
the value of the pressure P2 can be modulated and specifically controlled by supplying a differentiated power to said first compressor thanks to said first motor, making it possible to modulate and control the power supplied to the various compressors in a differentiated manner and therefore to vary the value of P2.
said pressure P2 is varied in a controlled manner by supplying power in a controlled manner to said first compressor with said first motor, so that the energy consumed for switching on.
implementation of the process (Ef) is minimal, preferably when the composition of the natural gas to be liquefied varies.
This process is more particularly advantageous because it thus makes it possible, by modulating and specifically controlling the value of the pressure P2 of said third flow, to modify and optimize the operating point of the process, namely to minimize the energy consumed and therefore to increase the efficiency in particular.
the composition of the natural gas to be liquefied varies.
said first motor provides at least 3%, preferably from 3 to 30% of the total power supplied to all of said compressors used, said gas turbine providing 97 to 70% of the power. total power supplied.
a conventional liquefaction unit is dimensioned in relation to the power of the gas turbines available, high power turbines commonly being 25MW, or even 30MW when they are intended to be installed on a floating support. Fixed gas turbines installed on land can reach maximum powers of 90-100MW.
the overall power is always the same, but in this case the efficiency of the assembly is improved, which represents a gain in energy consumed for the same power. overall, relative to a power injection at the second engine M2.
This first variant embodiment is advantageous in that it allows for the most compact installation in terms of size on board the floating support.
This second variant embodiment is advantageous in terms of thermodynamic efficiency and production capacity since a maximum capacity turbine available on the market can then be used advantageously as a gas turbine, that is to say 25-30MW in the case of gas turbine.
turbines intended to be installed on a floating support plus a second electric motor, for example from 5 to 10 MW, connected to the second compressor, the overall power of the second motor and third motor (gas turbine) then being 30 to 40MW, therefore vastly superior to that of the largest gas turbines available on the market and intended for floating supports.
the second engine can also be a gas turbine, preferably of identical power to the main gas turbine, which then makes it possible to achieve an overall power of 50 to 60 MW.
the method according to the invention makes it possible, by varying the pressure P2 by supplying energy to said first compressor using said first motor, to implement a minimum total energy Ef consumed in the method of less than 21.5 kW x day / t, more particularly from 18.5 to 20.5 kW x day / t of liquefied gas produced.
said refrigerant gas comprises nitrogen.
said refrigerant gas consists of a single gas chosen from nitrogen, hydrogen and neon.
neon is preferred in view of the greater explosion risk of hydrogen and the fact that hydrogen may have a certain propensity to percolate through elastomeric seals and even through low metal walls. thickness.
the PFD Process Flow Diagram
the process comprises compressors C1, C2 and C3, expansion valves E1 and E2, intercoolers H1 and H2 as well as cryogenic exchangers EC1, EC2 and EC3.
the heat exchangers consist, in a known manner, of at least two fluid circuits juxtaposed but not communicating with each other at the level of said fluids, the fluids circulating in said circuits exchanging heat throughout the path within said exchanger thermal.
a regulator achieves a pressure drop of a fluid or a gas and is represented by a symmetrical trapezoid, the small base of which represents the inlet 10a (high pressure), and the large base represents the outlet 10b (low pressure) as shown on figure 1 with reference to the regulator E2, said regulator can be a simple reduction in the diameter of the pipe, or else an adjustable valve, but in the case of the liquefaction process according to the invention, the regulator is generally a turbine intended to recover mechanical energy during said expansion, so that this energy is not lost.
a compressor increases the pressure of a gas and is represented by a symmetrical trapezoid, the large base of which represents the inlet 11a (low pressure), and the small base represents the outlet 11b ( high pressure) as shown on figure 1 with reference to compressor C2, said compressor generally being a turbine or a piston compressor, or else a scroll compressor.
the compressors C1 and C2 are mechanically connected to a motor M1 and M2 which can be either a heat engine, or an electric motor, or any other installation capable of providing mechanical energy.
T0 a temperature
T1 -50 ° C approximately.
the natural gas cools by releasing calories to the refrigerant gas, which then heats up and must permanently undergo a complete thermodynamic cycle in order to be able to extract in a manner continues natural gas calories entering AA.
the path of natural gas is represented on the left of the PFD, and said gas flows from top to bottom in the circuit Sg, the temperature decreasing from top to bottom, from a substantially ambient temperature T0 at the top in AA, to a temperature T3 of about -165 ° C at the bottom in DD.
thermodynamic cycle of the double-loop refrigerant gas corresponding to circuits S1 and S2.
the pressure levels in the main circuits are shown in thin lines for low pressure (P1 in circuit S1), in medium lines for intermediate pressure (P2), and in solid lines for high pressure (P3 in circuit S2).
phases 1, 2 and 3 are carried out by a low pressure loop P1 at very low temperature at the lower inlet of EC3.
a chiller H1, H2 can consist of a water exchanger, for example a sea or river water or cold air exchanger of the fan coil or cooling tower type, such as those used in nuclear power plants.
C1 and C2 are therefore arranged in parallel and operate between the medium pressure P'3 and the high pressure P3 on the entire flow from C3.
the refrigerant gas at the high outlet in AA of the circuit S1, at the level of the exchanger EC1 has a flow rate D: it is at low pressure P1 and at a temperature T'0 substantially lower than T0 and at ambient temperature. It is then compressed at C3 to pressure P'3 then passes through a cooler H1.
the flow rate fluid D is then separated into two parts of flow rates D1 'and D2' which respectively supply the compressors C1 (D1 ') and C2 (D2') operating in parallel.
the two streams at pressure P3 are then combined and then cooled substantially to ambient temperature T0 by passing through cooler H2.
This overall flow D then enters the top of the cryogenic exchanger EC1 at the level of the circuit S2, then at the exit of the first level, in BB, a large part of the flow rate D2 (D2 greater than D1) is extracted and directed. to the turbine E2 coupled to the compressor C2. The rest of the flow D1 passes through the second stage of the cryogenic exchanger EC2, then to the level CC is directed to the turbine E1 coupled to the compressor C1.
the flow D2 of refrigerant gas coming from the turbine E2 is at a pressure P1 and temperature T2 of about -120 ° C and is recombined within the circuit S1 to the flow D1 coming from the turbine E1 at the upper outlet. of the cryogenic exchanger EC3 in CC.
the separation of the second flow S2 into two parts of different flow rates D1 and D2 at the outlet BB of the first exchanger, preferably with D2 greater than D1, is advantageous because most of the energy consumed occurs in phase 2 within the second exchanger EC2.
the flow D of the circuit S1 is at the temperature T0 ′ substantially lower than the ambient temperature. Then, the flow D is again directed to the compressor C3 to continuously perform a new cycle.
compressors C1 and C2 operate in parallel and must ensure the highest level of pressure in the cycle.
the two compressors C1 and C2 process different refrigerant flow rates, respectively D1 'and D2', and are coupled directly to the turbines E1 and E2 which also process different flow rates, respectively D1 and D2.
D1 / D 5 to 35%, preferably 10 to 25%.
such an installation has an operating point which stabilizes itself at a given level of energy consumption Ef generally expressed in kW x day / t, that is to say in kW-day per tonne of LNG produced, or in kWh per kg of LNG produced, said operating point possibly being totally unstable. It is then very difficult to control the pressures of the high and low loops independently of one another. This may prove to be necessary in the case of variations in the composition of the natural gas to be liquefied. It is possible to modify the flows by locally constraining all or part of the D1-D'1-D2-D'1 flows, for example by creating localized pressure drops, but such arrangements lead to energy losses, therefore a drop in the overall efficiency of the liquefaction plant.
the diagram of the figure 4 illustrates the change in enthalpy H, expressed in kJ / kg of LNG produced, in a natural gas liquefaction process.
This diagram of the figure 4 is the result of a theoretical calculation relating to a natural gas comprising mainly methane (85%), the remainder (15%) consisting of nitrogen, ethane (C-2), propane (C-3) and butane (C-4).
the curve 50 comprising triangles illustrates the variations in the enthalpy H of the fluids circulating in co-current in the circuits Sg and S2 as a function of the temperature of the gas to be liquefied comprising the methane / LNG for an ideal virtual process.
Curve 51 corresponds to the variation in the enthalpy H of the refrigerant gas circulating in circuit S1 of the figure 1 , therefore represents the energy transferred to circuits Sg and S2 during the liquefaction process.
the area 52 between the two curves 50 and 51 represents the overall loss of energy consumed Ef in the liquefaction process: it is therefore sought to minimize this area so as to obtain the best efficiency.
curve 51 is no longer rectilinear, but is much closer to theoretical curve 50, which implies less losses, therefore improved efficiency, but the refrigerant phase change process is not suitable for liquefaction on board a floating support in a confined environment.
this part D2 of the second flow at the CC inlet of the second exchanger is recycled at an intermediate pressure P2 greater than P1 in a third circuit S3 independent of S1, S2, SG, and parallel to S1, that is to say to co -current of S1.
the entire flow of refrigerant gas D is at high pressure P3.
the flow is then cooled in a cooler H2 before circulating in the circuit S2, from top to bottom, through each of the two cryogenic exchangers EC1-EC2.
the refrigerant gas flow portion D2 is taken at BB at the outlet of the cryogenic exchanger EC1 and directed towards the inlet of the turbine E2, the remainder, that is to say the portion D1 of the flow of refrigerant gas being taken at DC at the outlet of the cryogenic exchanger EC2 and directed towards the inlet of the turbine E1.
a cooler H2 operating at pressure P'3 is installed between two compression stages, said cooler H2 treating all of the stream D.
the main advantage of the device according to the invention of the figure 2 lies in the possibility of optimizing the overall efficiency of the installations and of modifying at will the operating points of the various loops corresponding to the circuits S1-S2-S3, that is to say of minimizing the energy consumed by increasing or decreasing the power injected into one of the compressors C1-C2-C3, or by varying the distribution of the overall power Q injected into the system.
Curve 53 corresponds to the variation of the enthalpy H of the refrigerant circulating in circuits S1 and S3 of the figure 2 , therefore represents the energy transferred during the liquefaction process to circuits Sg and S2 of the figure 2 .
the surface 52 between the two curves 50 and 53 represents the overall energy loss in the liquefaction process with reference to the figure 2 : - We therefore seek to minimize this area so as to obtain the best performance.
the low point 54 of the curve 50 corresponding to P0 and T2 at the end of LNG liquefaction may vary by a few%.
the corresponding point 55 of the refrigerant gas circuit remains substantially fixed, and the surface 52, therefore the efficiency of the installation cannot be optimized.
the position of point 56 can be advantageously varied, as we know thus move optimally in the direction of point 54, which makes it possible to reduce to a minimum the surface of the area 52 between the curves 50 and 53, and thus to optimize in real time the efficiency of the installation of liquefaction, depending on the composition of natural gas.
the figure 3 shows the PFD diagram of a version of the invention exhibiting improved compactness compared to the method and installation of the figure 2 , in which the compressor C2 is integrated on the same shaft line as the compressor C3 and is driven by the gas turbine GT representing a mechanical energy input of 85 to 95% of the total energy Q.
the expansion turbine E2 is then connected on the one hand to compressor C2 and on the other hand to the gas turbine GT.
this compact version is advantageously justified in the event of a very limited available surface area, and in addition there are only two lines of rotating machine shafts and two compressors, whereas in the version with reference to the figure 2 , we must install three lines of rotating machine shafts and three compressors, which represents a significant additional cost, but provides greater flexibility in the fine adjustment of the various pressure loops, as well as a better final output, therefore a better profitability of installations in the long term, throughout the lifespan of the installations which exceeds 20 to 30 years, or even more.
the operating point in the case of the conventional method of figure 1 with pure nitrogen is located at 60.
the curve 70 (left portion) represents the variation of the energy yield as a function of the power injected into the process at the level of the motor M1 with reference to the figures 2 and 3 .
Point W1 corresponds to a power W1> 0 supplied by said motor M1.
Curve 90 represents the process according to figure 2 using a refrigerant gas composed of 100% nitrogen.
Point W1 corresponds to a power W1> 0 supplied by said motor M1.
the operating point W0 without energy input to the motor M1 corresponds, for a pure nitrogen process, to an energy consumption of approximately 21.25 kWxd / t, at the same pressure P1 of approximately 9 bars and a pressure P2 of about 11 bars: the energy efficiency is therefore improved by 7.06%.
the energy yield is shown as a function of the pressure P3, and as a function of the various variants of the invention, in particular in the case of a neon nitrogen mixture.
Points W0-W1-W2-W3-W4 correspond to the same levels of power injected into the motor M1 as described previously with reference to figures 5A - 6A .
P3 thus represents the maximum pressure of the system at the level of circuit S3: it increases in proportion to the power injected, as well as to the percentage of neon in the refrigerant gas mixture.
This minimum corresponds to the low point 71a of the curve 71 of the figure 5A , for a minimum energy consumption of approximately 19.4 kWxd / t, a pressure P1 of approximately 12.5 bars and a pressure P2 of approximately 33 bars.
the operating point W0 of the same curve 91 corresponding to a 20% mixture of neon, without energy input to the motor M1 corresponds to an energy consumption of approximately 20.45 kW x day / t , at the same pressure P1 of approximately 12.5 bars and a pressure P2 of approximately 17 bars, which illustrates the improvement in energy efficiency when the increase in the percentage of neon is combined with the increase in the power injected at motor M1.
the maximum pressure P3 is represented on the abscissa and the energy per unit mass of gas is on the ordinate.
the operating point of the conventional process with reference to the figure 1 is located in 60 on this figure 7A .
the efficiency of the installation can be varied according to curve 70 (20% neon) and other curves (40 - 50% of neon).
thermodynamic efficiency can be increased by increasing the maximum pressure.
a refrigerant gas consisting of 100% pure nitrogen by injecting part of the power at the level of the motor M1, and by operating at a pressure of approximately 68 bars, the consumption in energy drops to around 19.75 kWxd / t, which represents an efficiency gain of 7.28%.
the volume flow rates are reduced in proportion to the increase in said pressure: - the pipes are of smaller diameter, but their mechanical resistance, therefore their thickness, their weight and cost are increased by as much: - on the other hand, the footprint is reduced accordingly, which is very interesting in the case of installations in a confined environment such as on an anchored floating support at sea, or on an LNG carrier in the case of a boil-off reliquefaction unit.
compressors and turbines operating at higher pressure are much more compact.
cryogenic exchangers the increase in pressure also improves heat transfers, but the heat exchange surfaces are not reduced in the same proportion as in the case of pipes and compressors and turbines.
their weight increases significantly because they have to resist this increase in pressure.
the method according to the invention of figures 2-3 leads to installations having greater compactness and to a significant improvement in energy efficiency when the refrigerant gas is pure nitrogen, said energy efficiency being further improved when the refrigerant gas is a mixture of nitrogen and either neon, or hydrogen.
FIG 7A there is shown a performance diagram of a conventional process with reference to the figure 1 , and the method according to the invention of figures 2-3 using as refrigerant gas a mixture of nitrogen and neon, in which the maximum pressure P3 is represented on the abscissa and the energy per unit mass of gas is on the ordinate. Energy is represented in KW x day per tonne of natural gas (kW xd / t).
the operating point of the conventional process with reference to the figure 1 is located in 60 on this figure 7A .
the efficiency of the installation can be varied according to curve 61 with an optimum operating point 62 at approximately 68 bars, corresponding to an energy consumption of approximately 19.75 kWxd / t, which represents an efficiency gain of 7.28% compared to the operating point 60 of the conventional process.
the pressure can be increased, as shown on curve 70, without the gas mixture reaching its dew point, up to an optimum value 70a of approximately 88 bars and for a minimum energy consumption of approximately 19.4 kWxd / t, which represents a gain in thermodynamic efficiency of 1.77% compared to the operating point 62 of the process according to invention with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 8.92% over the operating point 60 of the conventional process.
the pressure can be increased, as shown on curve 71, without the gas mixture reaching its dew point, up to an optimum value 71a of approximately 118 bars and for a minimum energy consumption of approximately 19.15 kWxd / t, which represents a gain in thermodynamic efficiency of 3.04% compared to the operating point 62 of the process according to the invention with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 10.09% compared to the operating point 60 of the conventional process.
the pressure can be increased, as shown on curve 72, without the gas mixture reaching its dew point, up to an optimum value 72a of approximately 145 bars and for a minimum energy consumption of approximately 18.8 kWxd / t, which represents a gain in thermodynamic efficiency of 4.81% compared to the operating point 62 of the process according to the invention with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 11.74% compared to the operating point 60 of the conventional process.
a mixture of nitrogen and hydrogen is advantageously used as refrigerant gas.
the pressure can be increased, as shown on curve 80, without the gas mixture reaching its dew point, up to an optimum value 80a of around 94 bars and for a minimum energy consumption of around 19.2 kWxd / t, which represents a thermodynamic efficiency gain of 2.78% compared to the operating point 62 of the method according to the invention of figures 2-3 with a refrigerant gas composed of 100% nitrogen, and a thermodynamic efficiency gain of 9.86% compared to the operating point 60 of the conventional process of the figure 1 .
the pressure can be increased, as shown in curve 81, without the gas mixture reaching its dew point, up to at an optimum value 81a of approximately 140 bars and for a minimum energy consumption of approximately 18.8 kWxd / t, which represents a gain in thermodynamic efficiency of 4.81% compared to the operating point 62 of the process according to the invention of figures 2-3 with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 11.74% compared to the operating point 60 of the conventional process of the figure 1 .
the pressure can be increased, as shown on curve 82, without the gas mixture reaching its dew point, up to at an optimum value 82a of approximately 186 bars and for a minimum energy consumption of approximately 18.7 kWxd / t, which represents a gain in thermodynamic efficiency of 5.32% compared to the operating point 62 of the process according to the invention of figures 2-3 with a refrigerant gas composed of 100% nitrogen and a thermodynamic efficiency gain of 12.21% compared to the operating point 60 of the conventional process of the figure 1 .
the method according to the invention uses either a mixture of nitrogen and neon, or of nitrogen and hydrogen, and despite its slightly lower yield, the use of the mixture of nitrogen and neon will be preferred, because neon is an inert gas, while hydrogen is combustible and remains dangerous and difficult to operate, especially at high pressure in installations confined on board a floating medium.
hydrogen is a gas which percolates very easily through elastomeric seals and even in certain cases through metals, especially at very high pressure, and therefore the process according to the invention based on the use of a nitrogen-hydrogen mixture does not constitute the preferred version of the invention: the preferred version of the invention remains the use as refrigerant gas of a mixture of nitrogen and neon in the devices described with reference to the various figures.
curve 75 represents the variation in the yield of a conventional process according to the figure 1 , or its variants, depending on the percentage of neon gas in the refrigerant gas.
the operating point is at 70b, which corresponds to a maximum pressure P3 of approximately 63 bars and an energy consumption of approximately 20.45 kWxd / t, which represents a gain in efficiency thermodynamic of 3.76% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
the operating point is at 71b, which corresponds to a maximum pressure P3 of approximately 90 bars and an energy consumption of approximately 19.70 kWxd / t, which represents a gain in efficiency thermodynamic of 7.29% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
the operating point is at 72b, which corresponds to a maximum pressure P3 of approximately 120 bars and an energy consumption of approximately 19.35 kWxd / t, which represents a gain in efficiency thermodynamic of 8.94% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
the operating point is located at 80b, which corresponds to a maximum pressure P3 of approximately 68 bars and an energy consumption of approximately 20.2 kWxd / t, which represents a gain in thermodynamic efficiency of 4.94% compared to the point operation 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
the operating point is at 81b, which corresponds to a maximum pressure P3 of approximately 108 bars and an energy consumption of approximately 19.8 kWxd / t, which represents a gain of thermodynamic efficiency of 6.82% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
the operating point is located at 82b, which corresponds to a maximum pressure P3 of approximately 150 bars and an energy consumption of approximately 19 kWxd / t, which represents a gain of thermodynamic efficiency of 10.59% compared to the operating point 60 of the same conventional process with a refrigerant gas composed of 100% nitrogen.
a conventional liquefaction unit is dimensioned in relation to the powers of the gas turbines available, high power turbines are commonly 25MW.
the overall power is still 30MW, but in this case the efficiency of the assembly is improved and significantly reaches the value of 19.8 kW x day / t of LNG produced, which represents a gain of 6.59% for the same overall power of 30MW, compared to a power injection of 5MW at the level of the second motor M2, as detailed previously.
Said power input of 5 MW to the first motor M1 then represents 16.6% of the overall power and said efficiency (19.8 kW x day / t) corresponds substantially to point W2 of the diagram of the figure 7 .
the overall power is still 30MW, but in this case the efficiency of the assembly is improved and significantly reaches the value of 19.8 kW x day / t of LNG produced, which represents a gain of 6.59% for the same overall power of 30MW, compared to a power injection of 5MW at the level of the second motor M2, as detailed previously.
Said power input of 5 MW to the first motor M1 then represents 16.6% of the overall power and said efficiency (19.8 kW x day / t) corresponds substantially to point W2 of the diagram of the figure 7 .

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EP12731601.6A 2011-06-24 2012-06-22 Procédé de liquéfaction de gaz naturel a triple circuit ferme de gaz réfrigérant Active EP2724100B1 (fr)

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SI201231880T SI2724100T1 (sl)	2011-06-24	2012-06-22	Postopek za utekočinjanje zemeljskega plina z zaprtim trojnim krogotokom hladilnega plina
HRP20210341TT HRP20210341T1 (hr)	2011-06-24	2012-06-22	Postupak pretvaranja prirodnog plina u tekućinu sa trostrukim zatvorenim krugom rashladnog plina
RS20210238A RS61507B1 (sr)	2011-06-24	2012-06-22	Postupak za utečnjavanje prirodnog gasa sa trostrukim zatvorenim kolom rashladnog gasa

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FR1155595A FR2977015B1 (fr)	2011-06-24	2011-06-24	Procede de liquefaction de gaz naturel a triple circuit ferme de gaz refrigerant
PCT/FR2012/051428 WO2012175889A2 (fr)	2011-06-24	2012-06-22	Procédé de liquéfaction de gaz naturel a triple circuit ferme de gaz réfrigérant

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- 2012-06-22 WO PCT/FR2012/051428 patent/WO2012175889A2/fr not_active Ceased
- 2012-06-22 ES ES12731601T patent/ES2854990T3/es active Active
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Publication number	Publication date
WO2012175889A3 (fr)	2013-11-14
US20140190205A1 (en)	2014-07-10
CY1124080T1 (el)	2022-05-27
DK2724100T3 (da)	2021-02-15
SI2724100T1 (sl)	2021-04-30
RS61507B1 (sr)	2021-03-31
HUE053378T2 (hu)	2021-06-28
AU2012273829A1 (en)	2013-12-19
HRP20210341T1 (hr)	2021-04-30
FR2977015B1 (fr)	2015-07-03
US9557101B2 (en)	2017-01-31
ES2854990T3 (es)	2021-09-23
AU2012273829C1 (en)	2017-03-16
EP2724100A2 (fr)	2014-04-30
BR112013033341A2 (pt)	2017-01-31
PT2724100T (pt)	2021-02-18
AU2012273829B2 (en)	2016-05-26
FR2977015A1 (fr)	2012-12-28
WO2012175889A4 (fr)	2014-01-03
BR112013033341B1 (pt)	2021-02-09
WO2012175889A2 (fr)	2012-12-27

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