EP2673582B1 - Procédé et appareil de séparation cryogénique d'un débit riche en méthane - Google Patents
Procédé et appareil de séparation cryogénique d'un débit riche en méthane Download PDFInfo
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- EP2673582B1 EP2673582B1 EP12707884.8A EP12707884A EP2673582B1 EP 2673582 B1 EP2673582 B1 EP 2673582B1 EP 12707884 A EP12707884 A EP 12707884A EP 2673582 B1 EP2673582 B1 EP 2673582B1
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- nitrogen
- flow
- rich
- methane
- feed flow
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- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 title claims description 62
- 238000000034 method Methods 0.000 title claims description 17
- 238000000926 separation method Methods 0.000 title claims description 8
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 101
- 229910052757 nitrogen Inorganic materials 0.000 claims description 46
- 239000007789 gas Substances 0.000 claims description 27
- 239000001301 oxygen Substances 0.000 claims description 25
- 229910052760 oxygen Inorganic materials 0.000 claims description 25
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 24
- 239000007788 liquid Substances 0.000 claims description 20
- 238000004821 distillation Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims 1
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 8
- 239000000203 mixture Substances 0.000 description 8
- 239000003345 natural gas Substances 0.000 description 5
- 239000001569 carbon dioxide Substances 0.000 description 4
- 229910002092 carbon dioxide Inorganic materials 0.000 description 4
- 239000012535 impurity Substances 0.000 description 4
- 238000010586 diagram Methods 0.000 description 3
- 239000000243 solution Substances 0.000 description 3
- 238000001179 sorption measurement Methods 0.000 description 3
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 3
- 229910001873 dinitrogen Inorganic materials 0.000 description 2
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 239000012528 membrane Substances 0.000 description 2
- 239000000047 product Substances 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 239000012855 volatile organic compound Substances 0.000 description 2
- JVFDADFMKQKAHW-UHFFFAOYSA-N C.[N] Chemical compound C.[N] JVFDADFMKQKAHW-UHFFFAOYSA-N 0.000 description 1
- RWSOTUBLDIXVET-UHFFFAOYSA-N Dihydrogen sulfide Chemical compound S RWSOTUBLDIXVET-UHFFFAOYSA-N 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 239000002551 biofuel Substances 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 239000011449 brick Substances 0.000 description 1
- 230000003197 catalytic effect Effects 0.000 description 1
- 239000003245 coal Substances 0.000 description 1
- 230000000295 complement effect Effects 0.000 description 1
- 238000006477 desulfuration reaction Methods 0.000 description 1
- 230000023556 desulfurization Effects 0.000 description 1
- 230000037213 diet Effects 0.000 description 1
- 235000005911 diet Nutrition 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 229940110728 nitrogen / oxygen Drugs 0.000 description 1
- 239000010852 non-hazardous waste Substances 0.000 description 1
- 239000012264 purified product Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 238000001577 simple distillation Methods 0.000 description 1
- 239000012808 vapor phase Substances 0.000 description 1
- 239000002912 waste gas Substances 0.000 description 1
Images
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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0204—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the feed stream
- F25J3/0209—Natural gas or substitute natural gas
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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
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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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0233—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of CnHm with 1 carbon atom or more
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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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/0228—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream
- F25J3/0257—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream characterised by the separated product stream separation of nitrogen
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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
- F25J3/02—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream
- F25J3/04—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by rectification, i.e. by continuous interchange of heat and material between a vapour stream and a liquid stream for air
- F25J3/04521—Coupling of the air fractionation unit to an air gas-consuming unit, so-called integrated processes
- F25J3/04563—Integration with a nitrogen consuming unit, e.g. for purging, inerting, cooling or heating
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/02—Processes or apparatus using separation by rectification in a single pressure main column system
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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
- F25J2200/00—Processes or apparatus using separation by rectification
- F25J2200/70—Refluxing the column with a condensed part of the feed stream, i.e. fractionator top is stripped or self-rectified
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/40—Air or oxygen enriched air, i.e. generally less than 30mol% of O2
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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
- F25J2210/00—Processes characterised by the type or other details of the feed stream
- F25J2210/42—Nitrogen
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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
- 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"
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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
- F25J2260/00—Coupling of processes or apparatus to other units; Integrated schemes
- F25J2260/42—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery
- F25J2260/44—Integration in an installation using nitrogen, e.g. as utility gas, for inerting or purging purposes in IGCC, POX, GTL, PSA, float glass forming, incineration processes, for heat recovery or for enhanced oil recovery using nitrogen for cooling purposes
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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
- F25J2270/00—Refrigeration techniques used
- F25J2270/90—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration
- F25J2270/904—External refrigeration, e.g. conventional closed-loop mechanical refrigeration unit using Freon or NH3, unspecified external refrigeration by liquid or gaseous cryogen in an open loop
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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
- F25J2280/00—Control of the process or apparatus
- F25J2280/10—Control for or during start-up and cooling down of the installation
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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
- F25J2290/00—Other details not covered by groups F25J2200/00 - F25J2280/00
- F25J2290/90—Details about safety operation of the installation
Definitions
- the present invention relates to a method and apparatus for cryogenic separation of a methane-rich feed stream.
- the product contains less than 2% carbon dioxide and less than 2% for the total oxygen and nitrogen content.
- a flow rich in methane contains at least 30% methane.
- Biogas for example from a non-hazardous waste storage facility (ISDND), is a mixture of methane, carbon dioxide, nitrogen, oxygen and traces of other impurities such as water and hydrogen sulphide or volatile organic compounds (VOCs).
- ISDND non-hazardous waste storage facility
- VOCs volatile organic compounds
- the separation of CO 2 and CH 4 is preferably by permeation in a membrane system.
- Membranes do not, however, make it possible to economically separate methane from gases in the air, but sharp purity requirements must be met for the injection of biogas into the natural gas network. It is then necessary to find a complementary means to separate the methane from the gases of the air.
- adsorption system for this. This solution has several disadvantages such as low efficiency, many wear parts or adsorbent bottles and very bulky buffer capacity.
- a catalytic deoxygenator could solve this problem but gives rise to other problems such as the addition of an additional element in the process, the creation of water and C n H m or even coal or a potentially lower reliability of the assembly. biogas purification.
- An object of the present invention is to find a solution in the form of a process which always ensures an operation of the distillation column out of the flammable zone.
- feed rate denominates the flow entering the cold box, that is to say in the whole of the cryogenic distillation brick; this stream is already purified with CO 2 and other impurities mentioned above.
- feed composition is set is to enrich the nitrogen composition as it is plotted with the dotted line.
- a nitrogen enrichment is carried out by adding a nitrogen-rich flow rate to the distillation column. It is important to inject Nitrogen in the lower part of the column to avoid the flammability zone through the entire column.
- the apparatus may comprise a storage of the nitrogen-rich liquid connected to the means for sending the liquid to vaporize in the exchanger.
- figure 2 shows a simplified process diagram according to the invention.
- a flow of feed gas 1 which can be a biogas comprises between 30 and 50% of methane, with a CH 4 / CO 2 ratio between 1 and 2. It also contains air gases with a nitrogen / oxygen ratio. greater than 3.7 and is saturated with water.
- the gas 1 is purified by drying, by desulfurization and to remove the carbon dioxide it contains by permeation and / or adsorption in a treatment unit 2, so that it contains substantially only methane nitrogen and oxygen.
- a typical composition of the treated gas 4 could be 68% methane, 31% nitrogen and 3% oxygen.
- This feed gas 4 produced by the treatment unit 2 is cooled in a plate-and-fin type heat exchanger 3 at a pressure of between 6 and 15 bar.
- the gas 4 is sent to a tank condenser-reboiler 5 of a simple distillation column 6.
- the gas cools in the condenser-reboiler 5 and is at least partially condensed, while heating the tank of the column 6.
- the produced fluid 7 by condensing the gas 4 is expanded in a valve 8 at a pressure between 1.1 and 5 bar abs. then sent to the top of column 6 as liquid 9.
- the temperature of the liquid 9 must be greater than 90.7K to avoid the risk of solidifying the methane.
- This liquid then separates in column 6 to form an overhead gas containing 84% nitrogen and 5% oxygen.
- This gas 10 is heated in the exchanger 3 to form the waste gas 11.
- the vessel liquid 12 of the column 6 is withdrawn with a composition of less than 100 ppm of oxygen, traces of nitrogen and the remainder being methane .
- the tank liquid 12 is sent to the tank reboiler 5 where it partially vaporizes.
- the formed gas is returned to the bottom of the column via line 21.
- the remaining bottom liquid 13 vaporizes in exchanger 3 to form a pure methane gas product 14.
- a liquid nitrogen storage 16 is connected to the exchanger 3 by a pipe 17 to vaporize the liquid nitrogen.
- the vaporized nitrogen 18 is sent through an expansion valve 19 and the pipe 20 to the tank of the column 6, mixed with the vaporized methane 15 from the reboiler 5.
- the vaporized nitrogen contains at least 90% nitrogen, or even at least 95% nitrogen. Mixing the nitrogen with the vaporized methane makes it possible to better disperse the nitrogen in the column and to avoid the formation of flammable "pockets".
- the nitrogen may also come from an air separation apparatus producing nitrogen gas or a nitrogen gas network. Otherwise liquid nitrogen from an air separation apparatus can vaporize in the exchanger 3 to supply the gas 20.
- the feed gas can contain up to 10% oxygen or up to 5% oxygen.
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- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Mechanical Engineering (AREA)
- Thermal Sciences (AREA)
- General Engineering & Computer Science (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Separation By Low-Temperature Treatments (AREA)
Description
- La présente invention concerne un procédé et un appareil de séparation cryogénique d'un débit d'alimentation riche en méthane.
- Afin d'épurer un débit riche en méthane provenant d'une source organique, pour produire un produit épuré, il est nécessaire d'enlever les impuretés, telles que le dioxyde de carbone, l'oxygène et l'azote. Idéalement le produit contient moins de 2% de dioxyde de carbone et moins de 2% pour le contenu total en oxygène et en azote.
- Dans ce contexte, un débit riche en méthane contient au moins 30% de méthane.
- Tous les pourcentages de composition de ce document sont des pourcentages molaires.
- Le biogaz, provenant par exemple d'une installation de stockage de déchets non dangereux (ISDND), est un mélange de méthane, de dioxyde de carbone, d'azote, d'oxygène et des traces d'autres impuretés comme l'eau et le sulfure d'hydrogène ou des composants organiques volatils (COV).
- Pour une valorisation du méthane comme biocarburant ou pour l'injection dans le réseau de gaz naturel, une purification est nécessaire. Les impuretés présentes en traces peuvent être facilement arrêtées dans des lits d'adsorption ou d'autres procédés connus à l'homme de l'art.
- Quelques remarques concernant la présence d'oxygène dans le gaz naturel se trouvent dans
US-A-2006/0043000 . Le pourcentage d'oxygène dans le gaz naturel ne dépasse pas 0,1% d'après d'autres sources. - La séparation de CO2 et de CH4 se fait préférablement par perméation dans un système de membranes. Les membranes ne permettent cependant pas de séparer économiquement le méthane des gaz de l'air, or il faut respecter des exigences de pureté pointues pour l'injection du biogaz dans le réseau de gaz naturel. Il faut alors trouver un moyen complémentaire pour séparer le méthane des gaz de l'air. On trouve aujourd'hui sur le marché des offres utilisant un système d'adsorption pour cela. Cette solution présente plusieurs inconvénients comme un rendement faible, beaucoup des pièces d'usure ou des bouteilles d'adsorbant et des capacités tampon très volumineuses.
- Une autre solution pour la séparation est la distillation cryogénique tel que décrit dans
WO-A-09/004207 - Or, avec la présence d'oxygène dans le mélange à séparer, le problème d'inflammabilité du binaire méthane - oxygène se pose suite à la surconcentration d'oxygène au milieu de la colonne de distillation. Même de très petites quantités d'oxygène dans une alimentation loin d'être inflammable s'accumulent dans la colonne et peuvent créer une situation dangereuse.
- Ce problème n'a pas été abordé dans l'art antérieur, comme on voit de
US-A-2519955 où on va jusqu'à introduire délibérément un gaz contenant de l'oxygène (de l'air) dans une colonne de distillation de gaz naturel dépourvu d'oxygène. - Un désoxygénateur catalytique pourrait résoudre cette problématique mais engendre d'autres problèmes comme l'ajout d'un élément supplémentaire dans le procédé, la création d'eau et des CnHm voire du charbon ou une fiabilité potentiellement plus faible de l'ensemble de purification de biogaz.
- Un but de la présente invention est de trouver une solution en forme d'un procédé qui assure toujours une opération de la colonne de distillation hors de la zone d'inflammabilité.
- Dans ce qui suit le débit d'alimentation dénomme le flux entrant dans la boîte froide, c'est-à-dire dans l'ensemble de la brique de distillation cryogénique ; ce flux est déjà purifié de CO2 et d'autres impuretés citées ci-dessus.
- Dans le diagramme ternaire de la
Figure 1 , la zone triangulaire d'inflammabilité est hachée. La ligne continue trace la composition de la phase vapeur entre la tête de la colonne en bas à droite du diagramme et en cuve de la colonne où l'on trouve du méthane pur. On s'aperçoit facilement que cette ligne passe dans la zone d'inflammabilité. - Une possibilité d'éviter cette zone si la composition d'alimentation est fixée est un enrichissement de la composition en azote comme c'est tracé avec la ligne en pointillé.
- Selon l'invention, un enrichissement en azote est réalisé en rajoutant un débit riche en azote dans la colonne de distillation. Il est important d'injecter l'azote dans la partie inférieure de la colonne pour éviter la zone d'inflammabilité à travers toute la colonne.
- Selon un objet de l'invention, il est prévu un procédé selon la revendication 1.
- Selon d'autres caractéristiques optionnelles :
- le débit d'alimentation contient entre 65 et 97% de méthane ;
- le débit d'alimentation contient entre 3 et 35% en total d'azote et d'oxygène ;
- le débit d'alimentation contient entre 3 et 35% d'azote ;
- le débit riche en azote contient au moins 90% d'azote, voire au moins 95% d'azote ;
- le débit riche en azote est envoyé en cuve de la colonne de distillation ;
- le débit d'alimentation est envoyé à un condenseur-rebouilleur où il vaporise partiellement le liquide de cuve pour former un gaz vaporisé, le débit d'alimentation totalement ou partiellement liquéfié est envoyé du condenseur-rebouilleur à la colonne et le gaz vaporisé est mélangé avec le débit riche en azote ;
- le débit d'alimentation contient moins que 10% d'oxygène.
- Selon un autre objet de l'invention, il est prévu un appareil selon la revendication 9.
- L'appareil peut comprendre un stockage du liquide riche en azote relié aux moyens pour envoyer le liquide se vaporiser dans l'échangeur.
- L'invention sera décrite en plus de détail en se référant aux figures dont la
figure 2 montre un schéma simplifié de procédé selon l'invention. - Un débit de gaz d'alimentation 1 pouvant être un biogaz, comprend entre 30 et 50% de méthane, avec un rapport CH4/CO2 entre 1 et 2. Il contient également des gaz de l'air avec un rapport azote/oxygène supérieur à 3,7 et est saturé en eau. Le gaz 1 est épuré par séchage, par désulfurisation et pour éliminer le dioxyde de carbone qu'il contient par perméation et/ou par adsorption dans une unité de traitement 2, de sorte qu'il ne contient substantiellement plus que du méthane, de l'azote et de l'oxygène. Une composition typique du gaz traité 4 pourrait être 68% de méthane, 31% d'azote et 3% d'oxygène. Ce gaz d'alimentation 4 produit par l'unité de traitement 2 est refroidi dans un échangeur de chaleur 3 du type à plaques et à ailettes à une pression d'entre 6 et 15 bars. Le gaz 4 est envoyé à un condenseur-rebouilleur de cuve 5 d'une simple colonne de distillation 6. Le gaz se refroidit dans le condenseur-rebouilleur 5 et est au moins partiellement condensé, tout en chauffant la cuve de la colonne 6. Le fluide produit 7 en condensant le gaz 4 est détendu dans une vanne 8 à une pression entre 1,1 et 5 bars abs. puis envoyé en tête de la colonne 6 comme liquide 9. La température du liquide 9 doit être supérieure à 90,7K pour éviter le risque de solidifier le méthane.
- Ce liquide se sépare ensuite dans la colonne 6 pour former un gaz de tête 10 contenant 84% d'azote et 5% d'oxygène. Ce gaz 10 se réchauffe dans l'échangeur 3 pour former le gaz résiduaire 11. Le liquide de cuve 12 de la colonne 6 est soutiré avec une composition de moins de 100ppm d'oxygène, des traces d'azote et le reste étant du méthane. Le liquide de cuve 12 est envoyé au rebouilleur de cuve 5 où il se vaporise partiellement. Le gaz formé 15 est renvoyé à la cuve de la colonne par la conduite 21. Le liquide de cuve restant 13 se vaporise dans l'échangeur 3 pour former un produit de méthane gazeux pur 14.
- Un stockage d'azote liquide 16 est relié à l'échangeur 3 par une conduite 17 pour vaporiser l'azote liquide. L'azote vaporisé 18 est envoyé par une vanne de détente 19 et la conduite 20 à la cuve de la colonne 6, mélangé avec le méthane vaporisé 15 provenant du rebouilleur 5. L'azote vaporisé contient au moins 90% d'azote, voire au moins 95% d'azote. Le fait de mélanger l'azote avec le méthane vaporisé permet de mieux disperser l'azote dans la colonne et d'éviter la formation de « poches » inflammables.
- Pour démarrer la colonne 6, le stockage 16 contenant l'azote liquide pour permettre d'inerter la colonne.
- L'azote 20 peut également provenir d'un appareil de séparation d'air produisant de l'azote gazeux ou d'un réseau d'azote gazeux. Sinon de l'azote liquide d'un appareil de séparation d'air peut se vaporiser dans l'échangeur 3 pour fournir le gaz 20.
- De préférence, le gaz d'alimentation peut contenir jusqu'à 10% d'oxygène ou jusqu'à 5% d'oxygène.
Claims (10)
- Procédé de séparation cryogénique d'un débit d'alimentation (4) riche en méthane contenant de l'azote et entre 3 et 35% d'oxygène dans lequel :i) on refroidit (3) le débit d'alimentation pour produire un débit refroidi,ii) on envoie (9) au moins une partie du débit refroidi à une colonne de distillation (6),iii) on soutire (12) de la colonne de distillation un débit de cuve, le débit de cuve étant enrichi en méthane par rapport au débit d'alimentation,iv) on soutire (10) de la colonne de distillation un débit enrichi en oxygène par rapport au débit d'alimentation, etv) on vaporise un débit liquide riche en azote, provenant d'une source extérieure (16), par échange de chaleur avec le débit d'alimentation pour produire un débit gazeux riche en azote (18), caractérisé en ce que l'on envoie (20,21) le débit gazeux riche en azote à une partie inférieure de la colonne de distillation pour participer à la distillation.
- Procédé selon la revendication 1, dans lequel le débit d'alimentation (4) contient entre 65 et 97% de méthane.
- Procédé selon l'une des revendications précédentes, dans lequel le débit d'alimentation (4) contient entre 3 et 35% en total d'azote et d'oxygène.
- Procédé selon l'une des revendications 1 ou 2, dans lequel le débit d'alimentation (4) contient entre 3 et 35% d'azote.
- Procédé selon l'une des revendications précédentes, dans lequel le débit riche en azote (20,21) contient au moins 90% d'azote, voire au moins 95% d'azote.
- Procédé selon l'une des revendications précédentes, dans lequel le débit riche en azote (20, 1) est envoyé en cuve de la colonne de distillation (6).
- Procédé selon l'une des revendications précédentes, dans lequel le débit d'alimentation est envoyé à un condenseur-rebouilleur (5) où il vaporise partiellement le liquide de cuve pour former un gaz vaporisé, le débit d'alimentation totalement ou partiellement liquéfié est envoyé du condenseur-rebouilleur à la colonne et le gaz vaporisé est mélangé avec le débit riche en azote.
- Procédé selon l'une des revendications précédentes dans lequel le débit d'alimentation contient moins que 10% d'oxygène.
- Appareil de séparation cryogénique d'un débit d'alimentation riche en méthane contenant de l'oxygène et de l'azote comprenant :i) un échangeur de chaleur (3) pour permettre le refroidissement du débit d'alimentation pour produire un débit refroidi,ii) un condenseur-rebouilleur (5),iii) une colonne de distillation (6) et des moyens pour envoyer au moins une partie du débit refroidi au condenseur-rebouilleur,iv) des moyens (12) pour soutirer de la colonne de distillation un liquide enrichi en méthane par rapport au débit d'alimentation et pour l'envoyer au condenseur-rebouilleur,v) des moyens (13) pour soutirer du condenseur-rebouilleur un liquide riche en méthane et pour l'envoyer à l'échangeur,vi) des moyens (15) pour soutirer du condenseur-rebouilleur un gaz riche en méthane et pour le renvoyer en cuve de la colonne,vii) des moyens (10) pour soutirer de la colonne de distillation un débit enrichi en oxygène et éventuellement en azote par rapport au débit d'alimentation,viii) des moyens (17) pour envoyer un liquide riche en azote se vaporiser dans l'échangeur pour former un débit gazeux riche en azote, caractérisé en ce qu'il comprend des moyens (18,21) pour envoyer le débit gazeux riche en azote à la cuve de la colonne (6) mélangé avec le gaz riche en méthane pour participer à la distillation.
- Appareil selon la revendication 9, comprenant un stockage (16) du liquide riche en azote relié aux moyens pour envoyer le liquide se vaporiser dans l'échangeur.
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR1151013A FR2971332B1 (fr) | 2011-02-09 | 2011-02-09 | Procede et appareil de separation cryogenique d'un debit riche en methane |
PCT/FR2012/050269 WO2012107688A2 (fr) | 2011-02-09 | 2012-02-08 | Procédé et appareil de séparation cryogénique d'un débit riche en méthane |
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EP2673582A2 EP2673582A2 (fr) | 2013-12-18 |
EP2673582B1 true EP2673582B1 (fr) | 2018-10-10 |
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EP12707884.8A Active EP2673582B1 (fr) | 2011-02-09 | 2012-02-08 | Procédé et appareil de séparation cryogénique d'un débit riche en méthane |
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US (1) | US10132562B2 (fr) |
EP (1) | EP2673582B1 (fr) |
FR (1) | FR2971332B1 (fr) |
WO (1) | WO2012107688A2 (fr) |
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FR3051892B1 (fr) | 2016-05-27 | 2018-05-25 | Waga Energy | Procede de separation cryogenique d'un debit d'alimentation contenant du methane et des gaz de l'air, installation pour la production de bio methane par epuration de biogaz issus d'installations de stockage de dechets non-dangereux (isdnd) mettant en œuvre le procede |
SG11202000720TA (en) * | 2017-08-24 | 2020-03-30 | Exxonmobil Upstream Res Co | Method and system for lng production using standardized multi-shaft gas turbines, compressors and refrigerant systems |
FR3075660B1 (fr) * | 2017-12-21 | 2019-11-15 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Procede de distillation d'un courant gazeux contenant de l'oxygene |
FR3075658B1 (fr) * | 2017-12-21 | 2022-01-28 | Air Liquide | Procede de limitation de la concentration d'oxygene contenu dans un courant de biomethane |
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US2519955A (en) * | 1946-09-03 | 1950-08-22 | Shell Dev | Production of hydrocarbon-oxygen mixtures |
GB1482196A (en) * | 1973-09-27 | 1977-08-10 | Petrocarbon Dev Ltd | Upgrading air-contaminated methane gas compositions |
US4878932A (en) * | 1989-03-21 | 1989-11-07 | Union Carbide Corporation | Cryogenic rectification process for separating nitrogen and methane |
US5067976A (en) * | 1991-02-05 | 1991-11-26 | Air Products And Chemicals, Inc. | Cryogenic process for the production of an oxygen-free and methane-free, krypton/xenon product |
DE4425712C2 (de) * | 1994-07-20 | 1999-03-11 | Umsicht Inst Umwelt Sicherheit | Verfahren zur Anreicherung des Methangehaltes eines Grubengases |
MY117899A (en) * | 1995-06-23 | 2004-08-30 | Shell Int Research | Method of liquefying and treating a natural gas. |
DE19823526C1 (de) * | 1998-05-26 | 2000-01-05 | Linde Ag | Verfahren zur Xenongewinnung |
US6843973B2 (en) * | 2002-05-01 | 2005-01-18 | Air Products And Chemicals | Krypton and xenon recovery system |
ATE424541T1 (de) * | 2004-08-24 | 2009-03-15 | Advanced Extraction Technol | Kombinierte verwendung von externen und internen lösungsmitteln in leichte, mittelschwere und schwere komponenten enthaltenden prozessgasen |
DE102007010032A1 (de) * | 2007-03-01 | 2008-09-04 | Linde Ag | Verfahren zum Abtrennen von Stickstoff aus verflüssigtem Erdgas |
FR2917489A1 (fr) * | 2007-06-14 | 2008-12-19 | Air Liquide | Procede et appareil de separation cryogenique d'un debit riche en methane |
-
2011
- 2011-02-09 FR FR1151013A patent/FR2971332B1/fr active Active
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2012
- 2012-02-08 WO PCT/FR2012/050269 patent/WO2012107688A2/fr active Application Filing
- 2012-02-08 EP EP12707884.8A patent/EP2673582B1/fr active Active
- 2012-02-08 US US13/983,335 patent/US10132562B2/en active Active
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US20130312457A1 (en) | 2013-11-28 |
FR2971332A1 (fr) | 2012-08-10 |
WO2012107688A2 (fr) | 2012-08-16 |
FR2971332B1 (fr) | 2017-06-16 |
EP2673582A2 (fr) | 2013-12-18 |
WO2012107688A3 (fr) | 2014-07-24 |
US10132562B2 (en) | 2018-11-20 |
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