WO2023052983A1 - Procédé de givrage du dioxyde de carbone contenu dans du méthane liquide - Google Patents
Procédé de givrage du dioxyde de carbone contenu dans du méthane liquide Download PDFInfo
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- WO2023052983A1 WO2023052983A1 PCT/IB2022/059164 IB2022059164W WO2023052983A1 WO 2023052983 A1 WO2023052983 A1 WO 2023052983A1 IB 2022059164 W IB2022059164 W IB 2022059164W WO 2023052983 A1 WO2023052983 A1 WO 2023052983A1
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- methane
- separator
- carbon dioxide
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims abstract description 411
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 312
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 155
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 155
- 239000007788 liquid Substances 0.000 title claims abstract description 132
- 238000000034 method Methods 0.000 title claims abstract description 50
- 239000012071 phase Substances 0.000 claims abstract description 69
- 238000000926 separation method Methods 0.000 claims abstract description 32
- 239000007787 solid Substances 0.000 claims abstract description 32
- 238000000605 extraction Methods 0.000 claims abstract description 24
- 238000001914 filtration Methods 0.000 claims abstract description 9
- 239000007790 solid phase Substances 0.000 claims abstract description 4
- 239000007791 liquid phase Substances 0.000 claims description 20
- 238000010257 thawing Methods 0.000 claims description 17
- 239000012530 fluid Substances 0.000 claims description 8
- 239000008247 solid mixture Substances 0.000 claims description 7
- 238000005259 measurement Methods 0.000 claims description 6
- 239000003638 chemical reducing agent Substances 0.000 claims description 4
- 239000011159 matrix material Substances 0.000 claims description 4
- 230000008016 vaporization Effects 0.000 claims description 4
- 238000010438 heat treatment Methods 0.000 claims description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims 1
- QUWBSOKSBWAQER-UHFFFAOYSA-N [C].O=C=O Chemical compound [C].O=C=O QUWBSOKSBWAQER-UHFFFAOYSA-N 0.000 claims 1
- 229910052799 carbon Inorganic materials 0.000 claims 1
- 239000007789 gas Substances 0.000 description 24
- 239000002826 coolant Substances 0.000 description 17
- 238000012546 transfer Methods 0.000 description 11
- 238000011144 upstream manufacturing Methods 0.000 description 8
- 239000003949 liquefied natural gas Substances 0.000 description 7
- 238000000859 sublimation Methods 0.000 description 6
- 230000008022 sublimation Effects 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- 239000003345 natural gas Substances 0.000 description 5
- ATUOYWHBWRKTHZ-UHFFFAOYSA-N Propane Chemical compound CCC ATUOYWHBWRKTHZ-UHFFFAOYSA-N 0.000 description 4
- 238000010926 purge Methods 0.000 description 4
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 3
- OTMSDBZUPAUEDD-UHFFFAOYSA-N Ethane Chemical compound CC OTMSDBZUPAUEDD-UHFFFAOYSA-N 0.000 description 3
- 238000001816 cooling Methods 0.000 description 3
- 229930195733 hydrocarbon Natural products 0.000 description 3
- 150000002430 hydrocarbons Chemical class 0.000 description 3
- 238000009434 installation Methods 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 239000000523 sample Substances 0.000 description 3
- 239000012808 vapor phase Substances 0.000 description 3
- 239000001273 butane Substances 0.000 description 2
- KDRIEERWEFJUSB-UHFFFAOYSA-N carbon dioxide;methane Chemical compound C.O=C=O KDRIEERWEFJUSB-UHFFFAOYSA-N 0.000 description 2
- 238000004891 communication Methods 0.000 description 2
- 238000010276 construction Methods 0.000 description 2
- IJDNQMDRQITEOD-UHFFFAOYSA-N n-butane Chemical compound CCCC IJDNQMDRQITEOD-UHFFFAOYSA-N 0.000 description 2
- OFBQJSOFQDEBGM-UHFFFAOYSA-N n-pentane Natural products CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- 239000001294 propane Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000000758 substrate Substances 0.000 description 2
- 238000009834 vaporization Methods 0.000 description 2
- 239000002028 Biomass Substances 0.000 description 1
- VGGSQFUCUMXWEO-UHFFFAOYSA-N Ethene Chemical compound C=C VGGSQFUCUMXWEO-UHFFFAOYSA-N 0.000 description 1
- 239000005977 Ethylene Substances 0.000 description 1
- 235000011089 carbon dioxide Nutrition 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 239000013078 crystal Substances 0.000 description 1
- 210000005045 desmin Anatomy 0.000 description 1
- 238000000855 fermentation Methods 0.000 description 1
- 230000004151 fermentation Effects 0.000 description 1
- 230000008014 freezing Effects 0.000 description 1
- 238000007710 freezing Methods 0.000 description 1
- 239000013529 heat transfer fluid Substances 0.000 description 1
- 230000000977 initiatory effect Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 238000005191 phase separation Methods 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 239000003507 refrigerant Substances 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
- 239000002904 solvent Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Classifications
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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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
- F25J3/061—Natural gas or substitute natural gas
- F25J3/0615—Liquefied 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/0635—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of CnHm with 1 carbon atom or more
-
- 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
- F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
- F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
- F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
- F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2239/00—Aspects relating to filtering material for liquid or gaseous fluids
- B01D2239/12—Special parameters characterising the filtering material
- B01D2239/1208—Porosity
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2239/00—Aspects relating to filtering material for liquid or gaseous fluids
- B01D2239/12—Special parameters characterising the filtering material
- B01D2239/1216—Pore size
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/20—Processes or apparatus using other separation and/or other processing means using solidification of components
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/24—Processes or apparatus using other separation and/or other processing means using regenerators, cold accumulators or reversible heat exchangers
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
-
- 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/84—Processes or apparatus using other separation and/or other processing means using filter
-
- 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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/66—Landfill or fermentation off-gas, e.g. "Bio-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
- F25J2220/00—Processes or apparatus involving steps for the removal of impurities
- F25J2220/60—Separating impurities from natural gas, e.g. mercury, cyclic hydrocarbons
- F25J2220/66—Separating acid gases, e.g. CO2, SO2, H2S or RSH
-
- 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
- F25J2235/00—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams
- F25J2235/60—Processes or apparatus involving steps for increasing the pressure or for conveying of liquid process streams the fluid being (a mixture of) hydrocarbons
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Definitions
- the invention relates to the extraction of carbon dioxide (CO2) contained in liquid methane.
- Natural gas and biogas from biomass i.e. obtained by fermentation of organic waste, largely contain methane with the formula CH4.
- Natural gas contains mainly methane but also, in smaller quantities, ethane (CsHe) , propane (CsHs), butane (C4H12) as well as hydrogen sulphide (H 2 S) and CO 2 .
- CsHe ethane
- propane CsHs
- C4H12 propane
- H 2 S hydrogen sulphide
- CO 2 carbon dioxide
- biogas contains hydrogen sulphide and CO 2 .
- the liquefaction of methane or natural gas requires cryogenic installations.
- the gas temperature is lowered to liquefaction temperatures below -160°C at atmospheric pressure.
- the method and the device which are the subject of the invention aim to reduce the CO2 content of methane to very low values, from 50 to 100 ppmv, starting from typical concentrations of the order of 3000 ppmv of CO2 in the liquid phase methane.
- Methane brought to its liquefaction temperature at atmospheric pressure, i.e. -161.5°C, and containing CO2 will be supersaturated with solid CO2 if the CO2 content is greater than 270 ppmv, as taught in the publication “Solid-liquid -vapor phase behavior of the methane-carbon dioxide system” by J. A DAVIS, Newell RODEWALD and Fred KURATA published by AICh E JOURNAL volume 8, Issue 4, September 1962.
- the object of the invention is to guarantee a residual CO2 content in liquid methane or LNG of less than 200 ppmv.
- US patent 201 2/1 25043 describes a process for the precipitation of CO2 by a jet of liquid methane.
- a first object of the invention is a method for extracting the carbon dioxide contained in liquid methane, the method comprising: a step of expanding a liquid methane whose carbon dioxide content is greater than 280 parts per million by volume, and in particular of the order of 3000 parts per million by volume (ppmv), the expansion being carried out from a pressure greater than 6 bars to a pressure of 1 bar, the temperature of the liquid methane thus expanded being -161.5°C approximately, methane vaporizing and carbon dioxide crystallizing during this expansion, to form a three-phase liquid-vapor-solid mixture of methane and carbon dioxide, the liquid methane obtained being supersaturated in carbon dioxide, the method comprising: a step of passing the gas phase of methane and the solid phase of carbon dioxide through a first liquid-solid-gas separator, with extraction of the solid carbon dioxide by filtration, and separation of the gaseous methane, to obtain a first phase of liquid methane, partially decarbonated, a step of transferring this first phase of liquid methane
- the method according to the invention has the following characteristics, combined where appropriate.
- the carbon dioxide content of the first phase of liquid methane, from the first separator is around 300 ppmv.
- the temperature of the second separator is ⁇ 176° C., the carbon dioxide content of the second phase of liquid methane, at the outlet of the second separator, being less than 50 ppmv.
- the method comprises a step of extracting the solid carbon dioxide deposited in the second separator, this extraction being carried out in the gas phase at a pressure of the order of 500 mbar.
- the method comprises a step of extracting the solid carbon dioxide deposited in the second separator, this extraction being carried out in the liquid phase at a pressure of the order of 6 bar.
- the method comprises a step of measuring the pressure drop on the liquid methane between the inlet and the outlet of the first separator.
- the first separator comprises two enclosures, each enclosure being provided with a micron filter for recovering solid carbon dioxide.
- the process includes a step of reheating the filters.
- the method comprises measuring the temperature of the fluid circulating in the filters, downstream of the filters, the extraction of the carbon dioxide being completed when this temperature exceeds a predetermined threshold value, advantageously of the order of 10° C. .
- a predetermined threshold value advantageously of the order of 10° C.
- the method comprises a step of measuring the pressure drop on the liquid methane between the inlet and the outlet of the second separator.
- the second separator is a tube-fin exchanger.
- the maximum speed of liquid methane in the channels formed by the inter-fin spaces of the second exchanger is of the order of 0.2 m/s.
- the second separator comprises two chambers
- the method comprises a step of heating a chamber when the icing of the carbon dioxide deposited in this chamber of the second separator is interrupted.
- the method comprises measuring the temperature of the fluid circulating in the enclosures, downstream of the enclosures, the defrosting of the carbon dioxide being completed when this temperature exceeds a predetermined threshold value.
- the methane flow is advantageously diverted towards the second enclosure of the second separator, the second separator thus operating alternately, one enclosure of the second separator being in phase of icing when the other enclosure of the second separator is in the defrosting phase.
- the invention relates, according to a second aspect, to a device for extracting the carbon dioxide contained in liquid methane, for the implementation of the method presented above, the device comprising: a reservoir of liquid methane whose content in carbon dioxide is of the order of 3000 parts per million by volume (ppmv), at a pressure greater than 6 bar; a pressure reducer downstream of the tank, to reduce the pressure of the liquid methane to a value of 1 bar, the temperature of the liquid methane thus expanded being approximately -161.5°C, to form a three-phase liquid-vapor- solid of methane and carbon dioxide, the liquid methane obtained being supersaturated with carbon dioxide; a first liquid-solid-gas separator, in which the three-phase liquid-vapor-solid mixture enters, with extraction of the solid carbon dioxide by filtration, and separation of the gaseous methane, to obtain a first phase of liquid methane, partially decarbonated; a second liquid-solid separator, into which enters the first phase of liquid methane at a temperature
- the two enclosures of the first separator are identical.
- the micron filter is a solid matrix, with a porosity of the order of 10 micrometers.
- the second separator comprises two enclosures, each enclosure being provided with a tube-fin exchanger.
- the saturated CO2 concentration is 279 ppmv in liquid methane at 1 bar and -161.5°C.
- the method according to the present invention exploits in particular this physical phenomenon.
- the stages of the process are advantageously as follows: the liquid methane at a pressure greater than 6 bars has a CO2 content of the order of 3000 ppm, the CO2 is therefore perfectly soluble therein, according to the table of J. A Davis and para. This liquid methane is expanded from this high pressure to 1 bar and -161.5°C, which is the saturation temperature at 1 bar.
- the methane gas phase and the solid CO2 phase pass through a liquid-solid-gas separator where the solid CO2 is extracted by filtration, the gaseous methane is separated from the liquid.
- This gaseous methane is advantageously returned upstream of the liquefier to be liquefied again.
- the liquid methane from this first separator will be decarbonized in a complementary way, in a second separator.
- the first stage of separation of the vapor phase and the liquid phase of the methane makes it possible to control a slow rate of circulation of this liquid phase.
- a two-phase liquid-vapor mixture intrinsically has a higher velocity than a single liquid phase, for the same constructive arrangement.
- the vaporization of about 20% of the liquid during the expansion leads to a ratio between the volume of the gas phase and the liquid phase, called vacuum ratio, greater than 95%.
- the flow is therefore easily turbulent, which is undesirable for solid-liquid separation.
- the liquid phase of methane at around -161°C is transferred to an enclosure where this liquid methane circulates at low speed on the fins of an exchanger whose temperature is below -170°C.
- the solid CO2 is deposited on the fins and the concentration of CO2 in the liquid methane at -170°C gradually becomes less than 100 ppm.
- the liquid methane of the enclosure where the solid CO2 has accumulated on the fins is purged, then the enclosure is evacuated, the tube-fin heat exchanger rises in temperature by the internal circulation of a heat transfer fluid at a temperature above -50°C if the CO2 is extracted in the liquid phase, or above -100°C if the CO2 is extracted in the gas phase at a pressure of approximately 500 absolute millibars.
- the device for extracting carbon dioxide (CO2) by icing in liquid methane with a CO2 content of the order of 3000 ppm comprises a methane tank at a pressure greater than 6 bars which is advantageously downstream of a device for liquefying methane at a pressure greater than 6 bars.
- a pressure reducer reduces the pressure of the liquid methane to 1 bar and -161.5°C.
- the three-phase liquid-vapor-solid mixture of methane and CO2 resulting from this expansion enters through the bottom of this first separation device where both a first filtration of the solid phase of CO2 in a solid matrix of porosity of the order of 10 micrometers, and the separation of the gas and liquid phases of methane.
- the methane gas phase containing about 7 ppm of CO2 will advantageously be recycled and liquefied again.
- the liquid methane phase containing about 300 ppm of CO2 is transferred by a pump to the second separation device.
- the first separation device comprises two identical enclosures for alternate operation of each enclosure: when the separation of the three phases takes place in one, the solid CO2 is sublimated in the other by circulation of gaseous methane at atmospheric pressure originating from the methane discharged by a methane compressor, which is upstream of the liquefaction exchanger, this methane liquefier feeds the reservoir described above.
- the combination of the methane expansion and the first separation device reduces the CO2 content of the liquid methane from 3000 ppm to approximately 300 ppm by filtration of the liquid, and separates the gas and liquid phases, one sucked by the compressor of methane, the other by a pump which transfers the liquid methane to the second separation device.
- the flow of liquid methane at atmospheric pressure and at a content of around 300 ppm circulates in one of the two enclosures of the second separation device.
- each enclosure of the second separation device comprises a tube-fin exchanger, the methane circulating in the multiple parallel channels formed by the inter-fin spaces of this exchanger.
- the maximum speed of the liquid methane is preferably of the order of 0.2 m/s to facilitate the deposit of solid CO2 on the fins and to avoid any tearing of the ice already formed.
- the surface temperature of the fins is progressively cooler, typically from ⁇ 165° C. to ⁇ 170° C., these temperatures being perfectly adjustable.
- the CO2 content goes from about 300 ppm to a value below 100 ppm, it suffices to lower the final temperature to -176°C to obtain a CO2 content of less than 50 ppm.
- the purified methane is stored in a tank and ready to be transported.
- the second device for separation by frosting of CO2 in the liquid methane phase preferably also operates alternately: when one exchanger is in the frosting phase, the other is in the defrosting phase, the extraction of the CO2 deposited on the fins can be carried out either in the gas phase or in the liquid phase.
- the device for separating methane and CO2 to obtain a final concentration of CO2 in liquid methane of less than 100 ppm advantageously comprises:
- a pressure reducer making it possible to reduce the pressure of the liquid methane to 1 bar and -161.5°C, the expansion producing a three-phase liquid-vapor-solid mixture, the solid being CO2;
- a first separation device comprising: two identical enclosures each with a micron filter, a two-phase mixture inlet pipe and two outlet pipes, one in the gas phase sucked by a biomethane compressor with an anti-droplet device, the another in the liquid phase equipped with a dip tube to avoid vapor bubbles;
- the separation of liquid methane and CO2 by icing and deicing is preferably also carried out alternately in two identical enclosures each containing a tube-fin exchanger where the liquid methane circulates at low speed so that the CO2 frosts on the fins.
- these exchangers are supplied with a coolant whose lowest temperature is below - 170°C coming from a cryogenic system.
- the device for separating methane and CO2 to obtain a final concentration of CO2 in liquid methane of less than 100 ppm also advantageously comprises:
- the purified methane transfer circuit from the enclosures to the storage tank is advantageously equipped with a pump and a flow meter, in order to check the emptying of the liquid methane before initiating the defrosting phase.
- the coolant circuit producing the cooling capacity is connected to a heat transfer circuit, which makes it possible to raise the temperature of the exchanger during defrosting from -170°C to -45°C during the defrosting phase. , which allows the sublimation and the extraction of the CO2 sublimated in the gas phase by the vacuum pump or the sublimation up to 5.2 bar then the liquefaction of the CO2 beyond this pressure of the triple point of the CO2.
- the device for separating methane and CO2 to obtain a final concentration of CO2 in liquid methane of less than 100 ppm also advantageously comprises:
- the complete device preferably comprises a central unit, capable of implementing the method as previously described.
- FIG. 1 is a schematic representation of a first device for separating a device for extracting carbon dioxide from the liquid phase of methane;
- FIG. 2 is a schematic representation of a second separation device of a device for extracting carbon dioxide from the liquid phase of methane.
- the device 1 for filtering and icing the CO2 contained in liquid methane or LNG comprises a first separation device 20 represented schematically in FIG. 1, and a second separation device 30, represented in FIG. 2.
- the methane leaving the first separation device 20 has a CO2 content of around 300 ppm, and a pump 141 will cause this methane to circulate in a line 14, towards the second separation device 30 .
- the device 1 comprises a liquid methane tank 10 at a pressure greater than 6 bar and whose CO2 concentration is of the order of 3000 ppm.
- the device 1 comprises a regulator 1 2 for reducing the pressure of the liquid methane to 1 bar, installed on a connection pipe 1 1 between the tank 1 0 and two enclosures 21, 22 of the first separation device 20.
- Each enclosure 21, 22 includes a micron filter 23,24.
- the pipe 1 1 Downstream of the regulator 1 2, the pipe 1 1 forms two branches 1 1 1, 1 1 2.
- the enclosures 21, 22 are respectively supplied with liquid methane by the branches 111, 112 and solenoid valves 113, 114 control the supply to each of these enclosures 21, 22.
- Solid CO2 is recovered by filters 23, 24.
- the methane in the gas phase is evacuated by a line 13 connected to the suction of a biomethane compressor, via a branch 21 1 for enclosure 21 and a branch 221 for enclosure 22.
- a valve 216 and a temperature sensor 214 are placed on branch 21 1 .
- a valve 226 and a temperature sensor 224 are placed on branch 221.
- An anti-droplet device 21 2 prevents the entrainment of droplets towards the compressor, for the enclosure 21 .
- an anti-droplet device 222 prevents droplets being carried over to the compressor, for enclosure 22.
- Methane in the liquid phase is sucked up by a pump 141 installed on line 14 which connects the first separator 20 to the second separator 30.
- This pump 141 sucks up the liquid coming from a branch 251 for the enclosure 21, or coming from a branch 252 for enclosure 22.
- Methane in the liquid phase is sucked up via a dip tube associated with each branch 251 and 252.
- Line 14 is provided with a flow meter 142, downstream of pump 141.
- Branch 251 is fitted with a valve 253.
- branch 252 is provided with a valve 254.
- a line 15 supplies the enclosures 21, 22 with hot gaseous methane, at about 50°C.
- On this line 15 is placed a regulator 16, upstream of two supply branches of the speakers 21, 22.
- Each of the two supply branches of the hot gaseous methane enclosures is provided with a valve 151, 152.
- the circulation of the methane flow is controlled by an automaton.
- the automaton will open the series of valves 1 13, 216, 253 when the methane circulates in the enclosure 21.
- the automaton will open the series of valves 1 14, 226, 254 when the methane circulates in the enclosure 22.
- Enclosure 21 is fitted with a differential pressure gauge 213 measuring the pressure loss between the common inlet of the three-phase mixture and the liquid outlet on branch 251, when the methane flow passes through enclosure 21.
- enclosure 22 is equipped with a differential pressure gauge 223 measuring the pressure loss between the common inlet of the three-phase mixture and the liquid outlet on branch 252, when the methane flow passes through enclosure 22.
- the automaton When the separation takes place in the enclosure 21 and the high pressure loss threshold indicated by the differential pressure gauge 213 is reached, then the automaton generates the following actions: passage of the methane flow from the enclosure 21 to the enclosure 22, by opening the series of valves 114, 226, 254 and closing of valves 113, 216, valve 253 remaining open so that pump 141 empties enclosure 21 of its liquid. Valve 253 is closed again when flowmeter 142 indicates a lower and constant flow rate value, the excess flow rate corresponding to the emptying of the volume of liquid extracted from enclosure 21 which is known by construction.
- the automaton opens the valves 21 6 and 1 51 and the regulator 16 installed on line 15, in order to circulate hot methane gas at around 50°C to sublimate the trapped CO2 in filter 23.
- the methane flow comes from the high pressure of the methane compressor, expanded by the regulator 16 and the filter rinsing flow 23 is mixed with the gas flow from branch 221 and these two flows are sucked in by the methane compressor, via the line 13.
- the separator is ready for the three-phase separation of the next cycle.
- the methane leaving the first separation device 20 has a CO2 content of the order of 300 ppm.
- the pump 141 will circulate this methane in the second separation device 30, shown schematically in Figure 2.
- the second separation device 30 comprises two enclosures 31, 32.
- Each enclosure 31, 32 houses a tube-fin exchanger 33, 34.
- Line 14 supplies enclosure 31 via a branch 31 1 , a valve 313 being arranged on this branch 31 1 , upstream of enclosure 31 .
- Line 14 supplies enclosure 32 via a branch 312, a valve 314 being arranged on this branch 312, upstream of enclosure 32.
- Exchanger 33 of enclosure 31 is supplied with coolant fluid at -170 °C by a refrigerant line 330.
- a valve 335 is arranged on line 330.
- a heat transfer circuit 331 is connected to line 330 downstream of valve 330. Heat transfer circuit 331 is provided with a valve 337.
- the exchanger 34 of the enclosure 32 is supplied with coolant fluid at -170° C. by a coolant line 320.
- a valve 326 is arranged on line 320.
- a heat transfer circuit 321 is connected to line 320 downstream of the valve 326.
- the heat transfer circuit 321 is provided with a valve 328.
- the exchanger 33 is supplied with coolant fluid at -170°C and the coolant leaves the exchanger 33 via a line 333 to a cryogenic system (not shown), after cooling the liquid methane in the exchanger 33.
- a temperature sensor 334 is mounted on line 333.
- the exchanger 34 is supplied with coolant fluid at -170° C. and the coolant leaves the exchanger 34 by a line 322 to a cryogenic system (not shown), after cooling the liquid methane in the exchanger 34.
- a temperature sensor 324 is mounted on line 322.
- the enclosures 31, 32 are connected to a liquid methane tank 50, by a line 350 on which is mounted a pump 351 and a flow meter 352.
- a valve 317 is downstream of the enclosure 31 and upstream of the tank 50, a valve 316 being downstream of enclosure 32 and upstream of reservoir 50.
- the enclosures 31, 32 are connected to a pressurization tank 43, by a line 44 on which a valve 41 2 is mounted.
- Line 44 is in communication with enclosure 31 by a branch 413 on which a valve 415 is mounted.
- Line 44 is in communication with enclosure 32 by a branch 414 on which a valve 416 is mounted.
- the enclosures 31, 32 are connected to a purge line 40 on which are mounted a vacuum pump 60, a discharge valve 431 and a vacuum gauge 432.
- the enclosures 31, 32 are also connected to a liquid CO2 recovery tank 42 by a line 420.
- a valve 41 7 is mounted on branch 41 9 of line 420.
- a valve 41 8 is mounted on branch 41 6 of line 420. Downstream of branches 416, 419, line 420 is provided with a valve 421 and a temperature sensor 423.
- the enclosures 31, 32 are each provided with a multifunction pressure sensor 31 8, for measuring the absolute pressure in each of the enclosures 31 and 32 and for measuring the differential pressure between the pressure measured on the inlet branch 31 1 and output branch 354 for enclosure 31 and input branch 31 2 and output branch 353 for enclosure 32.
- valves 313,317 are open and the valve 314 is closed.
- the liquid methane circulating at low speed cools on the fins of the tube-fin exchanger 33 and the CO2 freezes on the fins as the temperature drops on the exchanger 33.
- the purified methane is sucked in by pump 351 and stored in tank 50.
- valves 314, 316 are open and valve 313 is closed.
- the liquid methane circulating at low speed cools on the fins of the tube-fin exchanger 34 and the CO2 freezes on the fins as the temperature drops on the exchanger 34.
- the purified methane is sucked up by pump 351 and stored in tank 50.
- the defrosting phase is launched.
- the automaton performs the following actions: the valve 314 is closed, the pump 351 on the line 350 creates the additional depression which allows the emptying of the enclosure 32 of its purified liquid methane in the storage tank 50, the valve 316 is closed again when the flow meter 352 indicates a lower and constant flow value, the excess flow corresponding to the emptying of the volume of liquid extracted from the enclosure 32 which is known by construction .
- valve 416 as well as the overflow valve 431 are opened, the vacuum pump 60 of the vacuum line 40 is started and the residual atmosphere with residual vaporization of liquid methane is carried out until the pressure gauge vacuum 432 indicates a residual pressure below 1 mbar.
- the coolant circuit 320 is closed by the valve 326 and the heat transport circuit 321 is opened by the valve 328, the CO2 pressure rises in the enclosure 32 and is maintained at around 500 mbar by the vacuum pump 60 until that the temperature probe 324 installed on the coolant outlet line 322 indicates a temperature above 10°C.
- the discharge valve 431 is closed, the vacuum pump 60 is stopped, the defrosting is carried out in the same way by circulation of the coolant in the exchanger and when the pressure at the inside the enclosure 32 measured by the pressure sensor 316 reaches 5.2 bar, pressure of the triple point, the CO2 liquefies.
- the circulation of the coolant is stopped by closing the valve 328 when the temperature indicated by the measurement of the probe 324 of the circuit 322 is greater than 10°C.
- Line 44 will connect, by opening the valves 41 2, 416, the pressurization tank 43 at approximately 8 bar and the enclosure 32.
- the pressure in the enclosure 32 will increase from 5.2 bar to about 6 bar, pressure measured by the sensor 318, the automaton then opens the valves 418.421 so that the liquid CO2 is transferred to the tank 42 of CO 2 .
- valves 421, 41 8 are closed in the same way as the valve 412 , which again isolates the reservoirs 43, 42.
- the overflow valve 431 is open and it maintains a maximum pressure of 1.2 bar downstream to avoid a pressure surge at the suction of the vacuum pump 60.
- the pressure reaches 1 mbar measured by the vacuum gauge 432, the vacuum pump 60 is stopped, the valves 431 and 414 are closed.
- Enclosure 32 is ready to begin a new CO2 icing cycle in liquid methane.
- a first advantage of the method thus described is that it is not necessary to use solutions of all kinds to extract the CO2. Therefore, the device 1 is simplified.
- a second advantage is that it is no longer necessary to recycle substrates of all kinds, which are obtained in conventional washing installations.
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Abstract
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AU2022356471A AU2022356471A1 (en) | 2021-09-28 | 2022-09-27 | Method for frosting carbon dioxide contained in liquid methane |
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FRFR2110231 | 2021-09-28 | ||
FR2110231A FR3127557B1 (fr) | 2021-09-28 | 2021-09-28 | Procédé de givrage du dioxyde de carbone contenu dans du méthane liquide |
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WO2023052983A1 true WO2023052983A1 (fr) | 2023-04-06 |
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PCT/IB2022/059164 WO2023052983A1 (fr) | 2021-09-28 | 2022-09-27 | Procédé de givrage du dioxyde de carbone contenu dans du méthane liquide |
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AU (1) | AU2022356471A1 (fr) |
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Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3254496A (en) | 1962-04-05 | 1966-06-07 | Transp Et De La Valorisation D | Natural gas liquefaction process |
EP1167905A2 (fr) * | 2000-06-20 | 2002-01-02 | Air Products And Chemicals, Inc. | Procédé et dispositif pour enlever des composés volatiles d'un courant gazeux |
US20020174678A1 (en) * | 2001-05-04 | 2002-11-28 | Wilding Bruce M. | Apparatus for the liquefaction of natural gas and methods related to same |
US20120125043A1 (en) | 2009-09-09 | 2012-05-24 | Exxonmobile Upstream Research Company | Cryogenic system for removing acid gases from a hydrocarbon gas stream |
WO2016060777A2 (fr) * | 2014-10-16 | 2016-04-21 | General Electric Company | Système et procédé de liquéfaction du gaz naturel |
US20180224205A1 (en) * | 2017-02-06 | 2018-08-09 | Larry Baxter | Method for Condensing a CO2 Vapor Stream Beyond the Frost Point |
-
2021
- 2021-09-28 FR FR2110231A patent/FR3127557B1/fr active Active
-
2022
- 2022-09-27 AU AU2022356471A patent/AU2022356471A1/en active Pending
- 2022-09-27 WO PCT/IB2022/059164 patent/WO2023052983A1/fr active Application Filing
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3254496A (en) | 1962-04-05 | 1966-06-07 | Transp Et De La Valorisation D | Natural gas liquefaction process |
EP1167905A2 (fr) * | 2000-06-20 | 2002-01-02 | Air Products And Chemicals, Inc. | Procédé et dispositif pour enlever des composés volatiles d'un courant gazeux |
US20020174678A1 (en) * | 2001-05-04 | 2002-11-28 | Wilding Bruce M. | Apparatus for the liquefaction of natural gas and methods related to same |
US20120125043A1 (en) | 2009-09-09 | 2012-05-24 | Exxonmobile Upstream Research Company | Cryogenic system for removing acid gases from a hydrocarbon gas stream |
WO2016060777A2 (fr) * | 2014-10-16 | 2016-04-21 | General Electric Company | Système et procédé de liquéfaction du gaz naturel |
US20180224205A1 (en) * | 2017-02-06 | 2018-08-09 | Larry Baxter | Method for Condensing a CO2 Vapor Stream Beyond the Frost Point |
Non-Patent Citations (3)
Title |
---|
J.A DAVISNEWELL RODEWALDFRED KURATA: "Solid-liquid-vapor phase behavior of the methane-carbon dioxyde system", AICHE JOURNAL, vol. 8, September 1962 (1962-09-01) |
J.A DAVISNEWELL RODEWALDFRED KURATA: "Solid-liquid-vapor phase behavior of the methane-carbon dioxyde system", ALCHE JOURNAL, vol. 8, September 1962 (1962-09-01) |
MAURO RIVA: "thèse", 12 September 2016, ECOLE DES MINES DE PARIS, article "Procédé de purification du biométhane : étude thermodynamique des équilibres solide-liquide-vapeur de mélanges riches en méthane" |
Also Published As
Publication number | Publication date |
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AU2022356471A1 (en) | 2024-05-16 |
FR3127557B1 (fr) | 2024-01-26 |
FR3127557A1 (fr) | 2023-03-31 |
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