EP1446620B1 - Procede et installation de production d'helium - Google Patents
Procede et installation de production d'helium Download PDFInfo
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- EP1446620B1 EP1446620B1 EP02803043.5A EP02803043A EP1446620B1 EP 1446620 B1 EP1446620 B1 EP 1446620B1 EP 02803043 A EP02803043 A EP 02803043A EP 1446620 B1 EP1446620 B1 EP 1446620B1
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- helium
- liquid
- nitrogen
- unit
- 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
- F25J3/028—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 noble gases
- F25J3/029—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 noble gases of helium
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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
- F25J3/02—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
- 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
- F25J2200/74—Refluxing the column with at least a part of the partially condensed overhead 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
- F25J2205/00—Processes or apparatus using other separation and/or other processing means
- F25J2205/02—Processes or apparatus using other separation and/or other processing means using simple phase separation in a vessel or drum
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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
- F25J2215/00—Processes characterised by the type or other details of the product stream
- F25J2215/04—Recovery of liquid products
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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
- 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
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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
- F25J2245/00—Processes or apparatus involving steps for recycling of process streams
- F25J2245/02—Recycle of a stream in general, e.g. a by-pass stream
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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
- F25J2260/20—Integration in an installation for liquefying or solidifying a fluid stream
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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
- F25J2270/02—Internal refrigeration with liquid vaporising 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/14—External refrigeration with work-producing gas expansion 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
- F25J2270/00—Refrigeration techniques used
- F25J2270/42—Quasi-closed internal or closed external nitrogen refrigeration cycle
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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
- F25J2270/88—Quasi-closed internal refrigeration or heat pump cycle, if not otherwise provided
Definitions
- the present invention relates in the first place to a process for producing pure helium.
- the invention applies for example to the production of helium from a residue gas of natural gas liquefier, the waste gas containing, besides helium, methane and nitrogen.
- the pressures here are absolute pressures.
- the invention aims to meet this need in a particularly effective manner.
- the subject of the invention is a method according to claim 1.
- the invention also relates to a unit according to claim 8.
- Figure unique schematically shows a helium production facility according to the invention.
- the plant shown in the drawing comprises an impure helium production unit A and a unit B for purified helium purification.
- This unit B comprises a cryogenic part, which may be an apparatus for the cryogenic purification of helium and possibly an apparatus for liquefying pure helium.
- Unit A essentially comprises a feed compressor 1 with two stages, a heat exchange line 2, a distillation column 3 provided with a head condenser 4, a heat exchanger 5, two phase separators 6 and 7, and a closed nitrogen refrigeration cycle 8.
- Unit A produces impure helium at 25 bar (line 9), nitrogen gas at 7 bar (line 10), liquid nitrogen at 8 bar (line 11), a first waste W1 rich in water. methane (line 12), a second waste W2 rich in methane (line 13), and a residual W3 rich in nitrogen (line 14). All the cold parts of this unit A are contained in the same cold box 15 suitably thermally insulated.
- a mixture of low pressure feed at 3.9 bar, brought by a line 16 is compressed to 8 bar by the first stage of the compressor 1, and then it is compressed to 26 bars, that is to say slightly above the impure helium production pressure, together with a mixture of high-pressure feed, brought by line 17.
- the compressed mixture is cooled and partially condensed in the exchange line 2 and is introduced into the bottom of the column 3.
- the bottom liquid of this column is expanded in an expansion valve 18 at about 4 bar and introduced into the shell 19 condenser 4 to refrigerate it.
- the uncondensed fraction is an intermediate gas containing about 25% helium and 75% nitrogen, and traces of methane.
- This intermediate gas is cooled and partially condensed in the exchanger 5, then separated in two phases in the separator 6.
- the vapor from this separator contains about 70% helium. After heating to 5 and 2, this steam is the impure helium production unit A, recovered, after heating in 5 and 2, via the pipe 9. This gas will then be treated in the unit B purification, and possibly liquefaction, helium.
- a flow rate of the liquid contained in the shell 19 is drawn off by a pump 21, vaporized and heated in the exchange line 2 and then constitutes the other waste W2 rich in methane, which is discharged via the pipe 13.
- the liquid phase of the separator 6 contains about 99% nitrogen. After expansion at 8 bar in an expansion valve 22, this liquid is introduced into the separator 7.
- the liquid phase constitutes a production of liquid nitrogen from the unit A, conveyed via line 11, whereas the gaseous phase constitutes a residual W3 rich in nitrogen, about 95% nitrogen, which is evacuated via line 14.
- the nitrogen refrigeration cycle 8 is a closed variable rate cycle independent of the rest of the installation. It comprises a cycle compressor 23 and a 24-blower turbine assembly 25 coupled to each other.
- the ring nitrogen compressed in 23 to 15 bar and overpressed in 25 to 23 bar, is cooled in the line exchange 2 to an intermediate temperature level and expanded to 24 to 1.6 bar.
- the nitrogen thus cooled serves to cool the exchanger 5, then continues its heating in 2 and returns to the suction of the compressor 23.
- the cycle nitrogen flow is adjusted according to the flow of liquid nitrogen produced.
- This liquid nitrogen is at least partly sent via the pipe 11 to the unit B of purification / liquefaction, and possibly partially out of the installation via a production line 26 stitched on the pipe 11.
- Unit B fed with impure helium via line 9 and liquid nitrogen through line 11, produces pure helium, possibly liquid, via line 27, and a waste gas W4 via line 28.
- liquid nitrogen is integrated in the unit A and in particular in the cold box 15 thereof.
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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)
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- Separation By Low-Temperature Treatments (AREA)
Description
- La présente invention est relative en premier lieu à une procédé de production d'hélium pur.
- L'invention s'applique par exemple à la production d'hélium à partir d'un gaz résiduatre de liquéfacteur de gaz naturel, ce gaz résiduaire contenant, outre l'hélium, du méthane et de l'azote.
- Les pressions dont il est question ici sont des pressions absolues.
- Un procédé de ce type est décrit dans le
US-A-4 701 200 , où l'hélium impur est ensuite purifié par adsorption sélective PSA (Pressure Swing Adsorption ou adsorption à modulation de pression). - Lorsque l'hélium doit être purifié par voie cryogénique et/ou liquéfié, il existe un besoin de liquide cryogénique. L'invention a pour but de satisfaire ce besoin de façon particulièrement efficace.
- A cet effet, l'invention a pour objet un procédé selon la revendication 1.
- Ce procédé peut comporter une ou plusieurs des caractéristiques suivantes :
- le cycle frigorifique est un cycle à azote ;
- on enrichit en l'un desdits composants la phase liquide obtenue par la seconde condensation partielle, et on récupère le fluide résultant en tant que second produit ;
- ledit second produit est au moins partiellement liquide ;
- on réalise la condensation partielle du gaz de tête de la colonne par échange de chaleur avec du liquide de cuve de la colonne, préalablement détendu ;
- on ajoute au mélange d'alimentation une fraction du gaz résultant de la vaporisation dudit liquide de cuve détendu ; et
- la pression de distillation est sensiblement égale à la pression de production de l'hélium impur.
- L'invention a également pour objet une unité selon la revendication 8.
- Un exemple de mise en oeuvre de l'invention va maintenant être décrit en regard du dessin annexé, dont la
- Figure unique représente schématiquement uns installation de production d'hélium conforme à l'invention.
- L'installation représentée au dessin comprend une unité A de production d'hélium impure, et une unité B de purification de l'hélium impur. Cette unité B comporte une partie cryogénique, qui peut être un appareil de purification cryogénique de l'hélium et éventuellement un appareil de liquéfaction de l'hélium pur.
- L'unité A comprend essentiellement un compresseur d'alimentation 1 à deux étages, une ligne d'échange thermique 2, une colonne de distillation 3 munie d'un condenseur de tête 4, un échangeur de chaleur 5, deux séparateurs de phases 6 et 7, et un cycle frigorifique fermé 8 à azote.
- L'unité A produit de l'hélium impur sous 25 bars (conduite 9), de l'azote gazeux sous 7 bars (conduite 10), de l'azote liquide sous 8 bars (conduite 11),un premier résiduaire W1 riche en méthane (conduite 12), un second résiduaire W2 riche en méthane (conduite 13), et un résiduaire W3 riche en azote (conduite 14). L'ensemble des parties froides de cette unité A est contenu dans une même boîte froide 15 convenablement isolée thermiquement.
- En fonctionnement, un mélange d'alimentation basse pression sous 3,9 bars, amené par une conduite 16, est comprimé à 8 bars par le premier étage du compresseur 1, puis il est comprimé à 26 bars, c'est-à-dire légèrement au-dessus de la pression de production de l'hélium impur, en même temps qu'un mélange d'alimentation haute pression, amené par une conduite 17.
- Le mélange comprimé est refroidi et partiellement condensé dans la ligne d'échange 2 et est introduit en cuve de la colonne 3. Le liquide de cuve de cette colonne est détendu dans une vanne de détente 18 à environ 4 bars et introduit dans la calandre 19 du condenseur 4 pour réfrigérer celui-ci.
- Cette réfrigération provoque dans le condenseur 4 la condensation partielle du gaz de tête de la colonne. La fraction non condensée est un gaz intermédiaire contenant environ 25% d'hélium et 75% d'azote , et des traces de méthane.
- Ce gaz intermédiaire est refroidi et partiellement condensé dans l'échangeur 5, puis séparé en deux phases dans le séparateur 6.
- La vapeur issue de ce séparateur contient environ 70% d'hélium. Après réchauffement en 5 et en 2, cette vapeur constitue l'hélium impur de production de l'unité A, récupéré, après réchauffement en 5 puis en 2, via la conduite 9. Ce gaz sera ensuite traité dans l'unité B de purification, et éventuellement de liquéfaction, d'hélium.
- Le gaz riche en méthane qui résulte de la vaporisation dans la calandre 19, contenant encore de l'hélium, est réchauffé en 2. Une partie majoritaire de ce gaz est recyclé via une conduite 20 à l'aspiration du premier étage du compresseur 1, et le reste est évacué via la conduite 12 en tant que résiduaire W1 riche en méthane.
- Un débit du liquide contenu dans la calandre 19 est soutiré par une pompe 21, vaporisé et réchauffé dans la ligne d'échange 2 puis constitue l'autre résiduaire W2 riche en méthane, lequel est évacué via la conduite 13.
- Bien entendu, les deux flux riches en méthane peuvent être valorisées, notamment pour leur pouvoir calorifique.
- La phase liquide du séparateur 6 contient environ 99% d'azote. Après détente à 8 bars dans une vanne de détente 22, ce liquide est introduit dans le séparateur 7. La phase liquide constitue une production d'azote liquide de l'unité A, véhiculée via la conduite 11, tandis que la phase gazeuse constitue un résiduaire W3 riche en azote, à environ 95% d'azote, qui est évacué via la conduite 14.
- Comme représenté, une partie de l'azote liquide est vaporisé dans l'échangeur 5 pour réfrigérer celui-ci, puis, après réchauffement en 2, forme le flux d'azote gazeux de production récupéré via la conduite 10.
- Le cycle frigorifique à azote 8 est un cycle fermé à débit variable indépendant du reste de l'installation. Il comprend un compresseur de cycle 23 et un ensemble turbine 24-surpresseur 25 couplés l'un à l'autre.
- L'azote de cycle, comprimé en 23 à 15 bars et surpressé en 25 à 23 bars, est refroidi dans la ligne d'échange 2 jusqu'à un niveau de température intermédiaire et détendu en 24 à 1,6 bar. L'azote ainsi refroidi sert à réfrigérer l'échangeur 5, puis poursuit son réchauffement en 2 et retourne à l'aspiration du compresseur 23.
- Le débit d'azote de cycle est réglé en fonction du débit d'azote liquide produit. Cet azote liquide est au moins en partie envoyé via la conduite 11 à l'unité B de purification/liquéfaction, et éventuellement partiellement sorti de l'installation via une conduite de production 26 piquée sur la conduite 11.
- L'unité B, alimentée en hélium impur par la conduite 9 et en azote liquide par la conduite 11, produit de l'hélium pur, éventuellement liquide, via une conduite 27, et un gaz résiduaire W4 via une conduite 28.
- Ainsi, la production d'azote liquide est intégrée à l'unité A et notamment dans la boîte froide 15 de celle-ci.
Claims (12)
- Procédé de production d'hélium pur, dans lequel :- on met en oeuvre un procédé de production d'hélium impur à partir d'un mélange gazeux d'alimentation contenant de l'hélium, de l'azote et du méthane, dans une unité (A) du type dans laquelle :- on amène le mélange d'alimentation à une pression de distillation,- on refroidit le mélange d'alimentation sous cette pression de distillation, et on l'introduit en cuve d'une colonne de distillation (3),- on condense partiellement (en 4) le gaz de tête de la colonne,- on refroidit (en 5) la phase gazeuse résultante de façon à la condenser partiellement ; et- on récupère en tant qu'hélium impur produit la phase gazeuse qui résulte de cette seconde condensation partielle,- on produit en outre au moins de l'azote sous forme d'un produit liquide en mettant en oeuvre un cycle frigorifique fermé à débit variable (8) dont le débit est fonction du débit dudit produit liquide ; et- on envoie l'hélium impur et ledit produit liquide à une unité (B) de purification, et éventuellement de liquéfaction, d'hélium comportant une partie cryogénique.
- Procédé suivant la revendication 1, caractérisé en ce que le cycle frigorifique (8) est un cycle à azote.
- Procédé suivant la revendication 1 ou 2, caractérisé en ce qu'on enrichit en azote (en 7) la phase liquide obtenue par la seconde condensation partielle, et en ce qu'on récupère le fluide résultant en tant que second produit.
- Procédé suivant la revendication 3, caractérisé en ce que ledit second produit est au moins partiellement liquide.
- Procédé suivant l'une quelconque des revendications 1 à 4, caractérisé en ce qu'on réalise la condensation partielle du gaz de tête de la colonne (3) par échange de chaleur avec du liquide de cuve de la colonne préalablement détendu.
- Procédé suivant la revendication 5, caractérisé en ce qu'on ajoute au mélange d'alimentation une fraction du gaz résultant de la vaporisation dudit liquide de cuve détendu.
- Procédé suivant la revendication 6, caractérisé en ce que la pression de distillation est égale à la pression de production de l'hélium impur.
- Installation de production d'hélium pur, caractérisée en ce qu'elle comprend :- une unité (A) de production d'hélium impur à partir d'un mélange gazeux d'alimentation contentant de l'hélium, de l'azote et du méthane du type comprenant :- des moyens (1) pour amener le mélange d'alimentation à une pression de distillation,- une ligne d'échange thermique (2) pour refroidir le mélange d'alimentation sous cette pression de distillation,- une colonne de distillation (3) dont la cuve est reliée au bout froid de la ligne d'échange thermique et qui est munie d'un condenseur de tête (4),- un échangeur de chaleur (5) adapté pour refroidir et condenser partiellement la phase vapeur issue des passages de condensation du condenseur de tête (4),- un séparateur de phases (6) relié au bout froid de l'échangeur de chaleur (5),- des moyens de récupération de la phase vapeur issue du séparateur (6), en tant qu'hélium impur produit,- un cycle frigorifique fermé à débit variable (8) pour la production d'un débit variable d'un produit liquide, qui est de l'azote liquide ; et- une unité (B) de purification, et éventuellement de liquéfaction, d'hélium comportant une partie cryogénique, cette unité (B) étant alimentée par l'hélium impur produit par l'unité (A) et par ledit produit liquide.
- Installation suivant la revendication 8, caractérisée en ce que le cycle frigorifique (8) est un cycle à azote.
- Unité suivant l'une quelconque des revendications 8 ou 9, caractérisée en ce qu'elle comprend en outre des moyens (7) d'enrichissement en l'un desdits composants de la phase liquide issue du séparateur de phases (6), et des moyens (10, 11) pour récupérer le fluide résultant en tant que second produit.
- Unité suivant l'une quelconque des revendications 8, 9 ou 10, caractérisée en ce que la colonne (3) comporte des moyens (18) de détente de son liquide de cuve et d'envoi du liquide détendu dans des passages de vaporisation du condenseur de tête (4).
- Unité suivant la revendication 11, caractériséee en ce qu'elle comprend une conduite (20) de recyclage de gaz, contenu dans la calandre (19) du condenseur de tête (4), dans le mélange gazeux d'alimentation.
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0114589 | 2001-11-12 | ||
FR0114589A FR2832213B1 (fr) | 2001-11-12 | 2001-11-12 | Procede et installation de production d'helium |
PCT/FR2002/003450 WO2003042615A1 (fr) | 2001-11-12 | 2002-10-10 | Procede et installation de production d'helium |
Publications (2)
Publication Number | Publication Date |
---|---|
EP1446620A1 EP1446620A1 (fr) | 2004-08-18 |
EP1446620B1 true EP1446620B1 (fr) | 2016-12-14 |
Family
ID=8869292
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP02803043.5A Expired - Lifetime EP1446620B1 (fr) | 2001-11-12 | 2002-10-10 | Procede et installation de production d'helium |
Country Status (5)
Country | Link |
---|---|
US (1) | US20040255618A1 (fr) |
EP (1) | EP1446620B1 (fr) |
JP (1) | JP2005509831A (fr) |
FR (1) | FR2832213B1 (fr) |
WO (1) | WO2003042615A1 (fr) |
Families Citing this family (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE102005006408A1 (de) * | 2005-02-11 | 2006-08-24 | Linde Ag | Verfahren zum Abtrennen von Spurenkomponenten aus einem Stickstoff-reichen Strom |
US7437889B2 (en) * | 2006-01-11 | 2008-10-21 | Air Products And Chemicals, Inc. | Method and apparatus for producing products from natural gas including helium and liquefied natural gas |
US20080091527A1 (en) * | 2006-10-17 | 2008-04-17 | Silverbrook Research Pty Ltd | Method of charging for ads associated with predetermined concepts |
DE102008007925A1 (de) * | 2008-02-07 | 2009-08-13 | Linde Aktiengesellschaft | Verfahren zur Helium-Gewinnung |
CN101476813B (zh) * | 2009-01-21 | 2011-06-15 | 成都蜀远煤基能源科技有限公司 | 一种煤气化装置来原料气的分离方法和装置 |
WO2013171856A1 (fr) | 2012-05-16 | 2013-11-21 | 石油資源開発株式会社 | Procédé de traitement et dispositif de traitement pour gaz naturel |
FR3035195B1 (fr) * | 2015-04-17 | 2019-07-12 | L'air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude | Installation et procede de production d'helium liquide |
US10215488B2 (en) | 2016-02-11 | 2019-02-26 | Air Products And Chemicals, Inc. | Treatment of nitrogen-rich natural gas streams |
CN109297261B (zh) * | 2018-10-17 | 2023-06-30 | 浙江海畅气体股份有限公司 | 一种氖氦低温气体冷能回收装置 |
CN113686098B (zh) * | 2021-09-27 | 2022-07-01 | 西南石油大学 | 一种天然气液化及氦气回收方法 |
CN113883827B (zh) * | 2021-10-29 | 2023-03-03 | 四川空分设备(集团)有限责任公司 | 一种氦气纯化及液化系统 |
FR3133102A1 (fr) | 2022-02-25 | 2023-09-01 | Marc Grosman | Procédé de production d’hélium par fusion-fission contrôlée et déclenchée par lasers. |
Family Cites Families (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US1664412A (en) * | 1919-08-07 | 1928-04-03 | Linde Air Prod Co | Production of helium from natural gas |
US3021682A (en) * | 1960-10-12 | 1962-02-20 | Union Carbide Corp | Process and apparatus for purifying low boiling gases |
US3815376A (en) * | 1969-07-31 | 1974-06-11 | Airco Inc | Process and system for the production and purification of helium |
US3719053A (en) * | 1969-10-23 | 1973-03-06 | Phillips Petroleum Co | Liquefaction and purification system |
US4701200A (en) * | 1986-09-24 | 1987-10-20 | Union Carbide Corporation | Process to produce helium gas |
US4758258A (en) * | 1987-05-06 | 1988-07-19 | Kerr-Mcgee Corporation | Process for recovering helium from a natural gas stream |
US5329775A (en) * | 1992-12-04 | 1994-07-19 | Praxair Technology, Inc. | Cryogenic helium production system |
-
2001
- 2001-11-12 FR FR0114589A patent/FR2832213B1/fr not_active Expired - Fee Related
-
2002
- 2002-10-10 JP JP2003544402A patent/JP2005509831A/ja active Pending
- 2002-10-10 EP EP02803043.5A patent/EP1446620B1/fr not_active Expired - Lifetime
- 2002-10-10 US US10/495,556 patent/US20040255618A1/en not_active Abandoned
- 2002-10-10 WO PCT/FR2002/003450 patent/WO2003042615A1/fr active Application Filing
Non-Patent Citations (1)
Title |
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None * |
Also Published As
Publication number | Publication date |
---|---|
WO2003042615A1 (fr) | 2003-05-22 |
FR2832213A1 (fr) | 2003-05-16 |
FR2832213B1 (fr) | 2004-09-24 |
EP1446620A1 (fr) | 2004-08-18 |
US20040255618A1 (en) | 2004-12-23 |
JP2005509831A (ja) | 2005-04-14 |
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