EP0223669A1 - Process for maintaining the composition of a stored product constant in a low-temperature liquefied gas storage space - Google Patents

Process for maintaining the composition of a stored product constant in a low-temperature liquefied gas storage space Download PDF

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Publication number
EP0223669A1
EP0223669A1 EP86402321A EP86402321A EP0223669A1 EP 0223669 A1 EP0223669 A1 EP 0223669A1 EP 86402321 A EP86402321 A EP 86402321A EP 86402321 A EP86402321 A EP 86402321A EP 0223669 A1 EP0223669 A1 EP 0223669A1
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EP
European Patent Office
Prior art keywords
product
heat exchanger
storage
composition
leaving
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP86402321A
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German (de)
French (fr)
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EP0223669B1 (en
Inventor
Alain Boulanger
Walter Luyten
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Distrigaz SA
Francaise De Stockage Geologique "geostock" Ste
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Distrigaz SA
Francaise De Stockage Geologique "geostock" Ste
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Publication of EP0223669A1 publication Critical patent/EP0223669A1/en
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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B65—CONVEYING; PACKING; STORING; HANDLING THIN OR FILAMENTARY MATERIAL
    • B65D—CONTAINERS FOR STORAGE OR TRANSPORT OF ARTICLES OR MATERIALS, e.g. BAGS, BARRELS, BOTTLES, BOXES, CANS, CARTONS, CRATES, DRUMS, JARS, TANKS, HOPPERS, FORWARDING CONTAINERS; ACCESSORIES, CLOSURES, OR FITTINGS THEREFOR; PACKAGING ELEMENTS; PACKAGES
    • B65D90/00—Component parts, details or accessories for large containers
    • B65D90/22—Safety features
    • B65D90/30—Recovery of escaped vapours
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/0002—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the fluid to be liquefied
    • F25J1/0022—Hydrocarbons, e.g. natural gas
    • F25J1/0025—Boil-off gases "BOG" from storages
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/004—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by flash gas recovery
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/003—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production
    • F25J1/0032—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration"
    • F25J1/0045—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures characterised by the kind of cold generation within the liquefaction unit for compensating heat leaks and liquid production using the feed stream itself or separated fractions from it, i.e. "internal refrigeration" by vaporising a liquid return stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0201—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration
    • F25J1/0202—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using only internal refrigeration means, i.e. without external refrigeration in a quasi-closed internal refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J1/00—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures
    • F25J1/02—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process
    • F25J1/0221—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop
    • F25J1/0224—Processes or apparatus for liquefying or solidifying gases or gaseous mixtures requiring the use of refrigeration, e.g. of helium or hydrogen ; Details and kind of the refrigeration system used; Integration with other units or processes; Controlling aspects of the process using the cold stored in an external cryogenic component in an open refrigeration loop in combination with an internal quasi-closed refrigeration loop
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2210/00—Processes characterised by the type or other details of the feed stream
    • F25J2210/62—Liquefied natural gas [LNG]; Natural gas liquids [NGL]; Liquefied petroleum gas [LPG]
    • 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

Definitions

  • the present invention relates to a method for keeping the composition of the product constant in low temperature storage of liquefied natural gas.
  • Storage of liquefied natural gas, in particular underground storage, has an evaporation rate of around 0.5% per day, regardless of the nature of the rock mass in which the storage is carried out. This value corresponds to storage conditions at temperatures between -162 ° C and -100 ° C approximately.
  • the gas phase or gaseous sky, will be of a composition different from that of the liquid phase.
  • composition of the stored product determines its calorific value which itself determines, in the case of natural gas, the size of the burners supplied or their consumption.
  • the object of the present invention is to provide a method for keeping the composition of a liquefied gas constant in a repository.
  • a method for keeping the composition of a liquefied gas constant in a repository comprises removing the product stored in the gaseous atmosphere of the repository, that is to say in the gaseous phase, compressing it by a compressor, a first cooling of the product taken from a first heat exchanger, followed by a second cooling in a second heat exchanger, its expansion in a tank at such a temperature, leaving the second heat exchanger, that part of the product is in the liquid phase, the return of the said liquid phase to the storage, the gaseous phase of the product being in the said reservoir being returned to the inlet of the said compressor, after having passed through the said first heat exchanger to cool the product leaving the said compressor, the withdrawal in the liquid phase of product stored from said storage by a pump, the over-compression of said liquid phase taken from said storage by a pump bank, part of the product leaving said pump bank being passed through the second heat exchanger to cool the product leaving said first heat exchanger before joining the rest of the product leaving said battery of pumps to then be directed to the
  • the attached Figure is a block diagram of a device for implementing the method of the invention, in the case of underground storage.
  • an underground storage cavity 1 contains a stored product, for example liquefied natural gas, at a pressure between atmospheric pressure and a few bars.
  • a stored product for example liquefied natural gas
  • the gas phase 4 In the upper part of the cavity, above the surface 2 of the liquid phase 3, there is product in the gas phase 4, resulting from the evaporation of the liquid phase of the product.
  • the respective compositions of each of the two phases are different because the stored product is not pure and is composed of a mixture of pure substances, each having different evaporation conditions. This evaporation is caused by external heat inputs from the rock mass 5 and its environment.
  • the product is taken in the gas phase by means of a pipe 7 by a compressor 8 which compresses it to an adjustable pressure, of the order of 10 bars, depending on the operating conditions of the device.
  • the product is then brought to pass through a first heat exchanger 9 where it undergoes a first cooling, then through a second heat exchanger 10, where it undergoes a second cooling, and from where it leaves at a temperature such that after expansion in a reservoir 11 via, for example, a first valve 12 of the Joule-Thomson type, it occurs in said reservoir 11 mainly in a liquid phase which is returned to the underground storage cavity via a second control valve 13 and a pipe 14.
  • the product being in the gas phase in said tank 11 is caused to pass, via a third control valve 15 and a pipe 16, through said first heat exchanger 9 for cooling the compressed gas leaving said compressor 8, before being directed itself towards the inlet of said compressor 8 via a line 17 connected to line 7 to be recycled in the circuit which it has already traversed, until it presents itself in the liquid phase in said reservoir 11.
  • product is withdrawn from the liquid phase 3 stored in the underground cavity 1 by means of a pipe 18 by means of a pump 19, then it is supercharged by a battery of pumps 20 to a pressure such that the distribution network of the product outside can be supplied directly by said battery of pumps after vaporization, that is to say about 80 bars in the example of the attached Figure.
  • Part of the product leaving said pump bank 20 is passed into the second heat exchanger 10 to cool the compressed gas leaving the first heat exchanger 9.
  • said part of the product leaving said battery of pumps 20 enters the second heat exchanger 10 at a temperature in the region of - 150 ° C and leaves it at approximately -80 ° C.
  • the flow of product leaving said battery of pumps 20 and the proportion of this product entering the second heat exchanger 10 are adjustable by means of a fourth and a fifth control valves 21 and 22 used jointly, said fourth valve 21 being mounted in parallel with the second heat exchanger 10 and said fifth valve 22, themselves mounted successively in series starting from the outlet of said pump bank 20.
  • the outlets of the fourth and fifth control valves 21 and 22 are connected together on the general outlet which is intended to be connected to the product distribution network outside, after spraying.
  • the operating parameters such as the temperatures, pressures and flow rates of the product at the various stages of the process, depend, on the one hand, on the composition of the product and, on the other hand, on the conditions under which the installation, at which the method of the present invention is applied, is exploited.
  • a point clipping unit with which an aerial storage is associated is operated at atmospheric pressure and at a temperature of the order of - 160 ° C. Therefore, the maintenance of the composition of the product can be ensured by the method according to the present invention.
  • the storage receives the product stored by a large capacity liquefaction device and it is operated at atmospheric pressure at approximately - 160 ° C.
  • the required gas phase flow rate is then marginal compared to that of filling the repository and its influence on the composition of the product is negligible.
  • the underground storage is operated at a pressure which can vary between atmospheric pressure and a few bars but, in general, the associated equipment does not include a liquefaction unit.
  • the installation must be designed to dispatch the gas in the distribution network with a composition as constant as possible.
  • a device such as that of the example described with reference to the attached Figure is applicable to such an installation.

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

Abstract

Un procédé pour maintenir constante la composition d'un gaz liquéfié dans un stockage (1) comprend le prélèvement du produit stocké dans sa phase gazeuse au moyen d'un compresseur (8) qui le comprime à une pression adéquate. Après refroidissement dans un premier échangeur thermique (9) puis dans un deuxième échangeur thermique (10), la température finale est telle qu'après détente dans un réservoir (11), on obtient un liquide et une faible partie de gaz qui est recyclée à l'aspiration du compresseur (8) après avoir refroidi le gaz comprimé dans le premier échangeur thermique (9). De plus, du liquide (3) est prélevé dans le stockage (1) grâce à une pompe (19). Ce liquide est alors surcomprimé par une batterie de pompes (20) à une pression telle que le réseau de distribution puisse être alimenté directement après vaporisation. Une partie de ce liquide est prélevée pour faire subir au gaz sortant du premier échangeur thermique (9) son deuxième refroidissement dans le deuxième échangeur thermique (10).A method for keeping the composition of a liquefied gas constant in a storage (1) comprises removing the product stored in its gas phase by means of a compressor (8) which compresses it to an adequate pressure. After cooling in a first heat exchanger (9) then in a second heat exchanger (10), the final temperature is such that after expansion in a tank (11), a liquid and a small part of gas are obtained which is recycled to the suction of the compressor (8) after having cooled the compressed gas in the first heat exchanger (9). In addition, liquid (3) is taken from the storage (1) using a pump (19). This liquid is then supercharged by a battery of pumps (20) at a pressure such that the distribution network can be supplied directly after vaporization. Part of this liquid is withdrawn to subject the gas leaving the first heat exchanger (9) to its second cooling in the second heat exchanger (10).

Description

La présente invention concerne un procédé pour maintenir constante la composition du produit dans un stockage à basse température de gaz naturel liquefié.The present invention relates to a method for keeping the composition of the product constant in low temperature storage of liquefied natural gas.

Un stockage de gaz naturel liquefié, en particulier un stockage souterrain, présente un taux d'évaporation de l'ordre de 0,5% par jour, quelle que soit la nature du massif rocheux dans lequel le stockage est réalisé. Cette valeur correspond à des conditions de stockage à des températures comprises entre-162°C et-100°C environ.Storage of liquefied natural gas, in particular underground storage, has an evaporation rate of around 0.5% per day, regardless of the nature of the rock mass in which the storage is carried out. This value corresponds to storage conditions at temperatures between -162 ° C and -100 ° C approximately.

Compte-tenu du fait que le gaz naturel n'est pas un gaz pur mais un mélange de gaz, et que le stockage est diphasique, la phase gazeuse, ou ciel gazeux, sera d'une composition différente de celle de la phase liquide.Given the fact that natural gas is not a pure gas but a mixture of gases, and that the storage is two-phase, the gas phase, or gaseous sky, will be of a composition different from that of the liquid phase.

Or, pour maintenir des conditions de température et de pression de stockage sensiblement constantes, il est nécessaire de permettre, par une procédure quelconque, un certain taux d'évaporation, et donc de permettre une libération d'une partie de la phase gazeuse du stockage quasiment en permanence, pour compenser les apports de chaleur provenant, dans le cas d'un stockage souterrain, du massif rocheux environnant.However, to maintain substantially constant storage temperature and pressure conditions, it is necessary to allow, by any procedure, a certain rate of evaporation, and therefore to allow a release of part of the gaseous phase of storage. almost permanently, to compensate for heat input from, in the case of underground storage, the surrounding rock mass.

Dans le cas d'une unité dite d'écrêtement de pointes associée à un stockage aérien, les temps d'attente étant très longs, le phénomène d'enrichissement de la phase liquide en produits lourds décrit ci-dessus apparaît également, bien que le taux d'évaporation journalier soit moins élevé que dans le cas d'un stockage souterrain.In the case of a so-called tip clipping unit associated with overhead storage, the waiting times being very long, the phenomenon of enrichment of the liquid phase with heavy products described above also appears, although the daily evaporation rate is lower than in the case of underground storage.

Cette libération d'une partie de la phase gazeuse entraîne ainsi à terme une modification de la composition du produit stocké, qui peut, selon les cas, poser des problèmes importants auxquels il est nécessaire de trouver des solutions. Par exemple, la composition du produit stocké détermine son pouvoir calorifique qui lui-même détermine, dans le cas du gaz naturel, le dimensionnement des brûleurs alimentés ou leur consommation.This release of part of the gas phase thus eventually leads to a change in the composition of the stored product, which can, depending on the case, pose significant problems to which solutions must be found. For example, the composition of the stored product determines its calorific value which itself determines, in the case of natural gas, the size of the burners supplied or their consumption.

Le but de la présente invention est de proposer un procédé pour maintenir constante la composition d'un gaz liquéfié dans un stockage.The object of the present invention is to provide a method for keeping the composition of a liquefied gas constant in a repository.

Selon la présente invention, un procédé pour maintenir constante la composition d'un gaz liquéfié dans un stockage comprend le prélèvement de produit stocké dans le ciel gazeux du stockage, c'est-à-dire en phase gazeuse, sa compression par un compresseur, un premier refroidissement du produit prélevé dans un premier échangeur thermique, suivi d'un deuxième refroidissement dans un deuxième échangeur thermique, sa détente dans un réservoir à une température telle, en sortant du deuxième échangeur thermique, qu'une partie du produit soit en phase liquide, le retour de ladite phase liquide dans le stockage, la phase gazeuse de produit se trouvant dans ledit réservoir étant renvoyée à l'entrée dudit compresseur, après être passée dans ledit premier échangeur thermique pour refroidir le produit sortant dudit compresseur, le prélèvement en phase liquide de produit stocké depuis ledit stockage par une pompe, la surcompression de ladite phase liquide prélevée depuis ledit stockage par une batterie de pompes, une partie du produit sortant de ladite batterie de pompes étant passée dans le deuxième échangeur thermique pour refroidir le produit sortant dudit premier échangeur thermique avant de rejoindre le reste du produit sortant de ladite batterie de pompes pour être dirigée ensuite vers le réseau de distribution, et le contrôle des débits du produit, sous les différentes conditions de température, de pression et de phase, par une première, une deuxième et une troisième vannes de contrôle prévues respectivement entre le premier échangeur thermique et ledit réservoir, entre ledit réservoir et la cavité souterraine, et entre ledit réservoir et le premier échangeur thermique, et par une quatrième et une cinquième vannes de contrôle prévues respectivement entre ladite batterie de pompes et le réseau de distribution, et entre le deuxième échangeur thermique et le réseau de distribution.According to the present invention, a method for keeping the composition of a liquefied gas constant in a repository comprises removing the product stored in the gaseous atmosphere of the repository, that is to say in the gaseous phase, compressing it by a compressor, a first cooling of the product taken from a first heat exchanger, followed by a second cooling in a second heat exchanger, its expansion in a tank at such a temperature, leaving the second heat exchanger, that part of the product is in the liquid phase, the return of the said liquid phase to the storage, the gaseous phase of the product being in the said reservoir being returned to the inlet of the said compressor, after having passed through the said first heat exchanger to cool the product leaving the said compressor, the withdrawal in the liquid phase of product stored from said storage by a pump, the over-compression of said liquid phase taken from said storage by a pump bank, part of the product leaving said pump bank being passed through the second heat exchanger to cool the product leaving said first heat exchanger before joining the rest of the product leaving said battery of pumps to then be directed to the distribution network, and controlling the flow rates of the product, under different temperature, pressure and phase conditions, by a first, a second and a third control valves provided respectively between the first er heat exchanger and said tank, between said tank and the underground cavity, and between said tank and the first heat exchanger, and by a fourth and a fifth control valves provided respectively between said pump bank and the distribution network, and between the second heat exchanger and the distribution network.

D'autres caractéristiques et avantages de la présente invention apparaîtront mieux à la lecture de la description suivante donnée à titre d'exemple non limitatif des formes possibles de réalisation de l'invention, en regard de la figure ci-jointe, et qui fera bien comprendre comment l'invention peut être réalisée.Other characteristics and advantages of the present invention will appear better on reading the following description given by way of nonlimiting example of the possible embodiments of the invention, with reference to the attached figure, and which will do well understand how the invention can be realized.

La Figure ci-jointe est un schéma de principe d'un dispositif permettant de mettre en oeuvre le procédé de l'invention, dans le cas d'un stockage souterrain.The attached Figure is a block diagram of a device for implementing the method of the invention, in the case of underground storage.

Sur la Figure ci-jointe, une cavité souterraine de stockage 1 contient un produit stocké, par exemple du gaz naturel liquifié, sous une pression comprise entre la pression atmosphérique et quelques bars. Dans la partie supérieure de la cavité, au dessus de la surface 2 de la phase liquide 3, se trouve du produit en phase gazeuse 4, résultant de l'évaporation de la phase liquide du produit. Les compositions respectives de chacune des deux phases sont différentes car le produit stocké n'est pas pur et est composé d'un mélange de corps purs ayant chacun des conditions d'évaporation différentes. Cette évaporation est provoquée par les apports de chaleur extérieure provenant du massif rocheux 5 et de son environnement. C'est cette évaporation qui permet de maintenir sensiblement constante la température de stockage, à une température fonction de la pression de service, température qui peut être de l'ordre de - 125°C à - 160°C. La cavité est fermée en partie supérieure par un bouchon étanche 6 à travers duquel peuvent passer des canalisations.In the attached figure, an underground storage cavity 1 contains a stored product, for example liquefied natural gas, at a pressure between atmospheric pressure and a few bars. In the upper part of the cavity, above the surface 2 of the liquid phase 3, there is product in the gas phase 4, resulting from the evaporation of the liquid phase of the product. The respective compositions of each of the two phases are different because the stored product is not pure and is composed of a mixture of pure substances, each having different evaporation conditions. This evaporation is caused by external heat inputs from the rock mass 5 and its environment. It is this evaporation which makes it possible to maintain the storage temperature substantially constant, at a temperature which depends on the operating pressure, a temperature which can be of the order of - 125 ° C to - 160 ° C. The cavity is closed in the upper part by a tight plug 6 through which pipes can pass.

Selon la présente invention, le produit est prélevé en phase gazeuse au moyen d'une canalisation 7 par un compresseur 8 qui le comprime jusqu'à une pression réglable, de l'ordre de 10 bars, dépendant des conditions de fonctionnement du dispositif. Le produit est ensuite amené à passer dans un premier échangeur thermique 9 où il subit un premier refroidissement, puis dans un deuxième échangeur thermique 10, où il subit un deuxième refroidissement, et d'où il sort à une température telle qu'après détente dans un réservoir 11 par l'intermédiaire, par exemple, d'une première vanne 12 du type de Joule-Thomson, il se présente dans ledit réservoir 11 principalement en une phase liquide qui est retournée vers la cavité souterraine de stockage par l'intermédiaire d'une deuxième vanne de contrôle 13 et d'une canalisation 14. Le produit se trouvant en phase gazeuse dans ledit réservoir 11 est amené à passer, par l'intermédiaire d'une troisième vanne de contrôle 15 et d'une canalisation 16, dans ledit premier échangeur thermique 9 pour refroidir le gaz comprimé sortant dudit compresseur 8, avant d'être dirigé lui-même vers l'entrée dudit compresseur 8 par l'intermédiaire d'une canalisation 17 raccordée à la canalisation 7 pour être recyclé dans le circuit qu'il a déjà parcouru, jusqu'à ce qu'il se présente en phase liquide dans ledit réservoir 11.According to the present invention, the product is taken in the gas phase by means of a pipe 7 by a compressor 8 which compresses it to an adjustable pressure, of the order of 10 bars, depending on the operating conditions of the device. The product is then brought to pass through a first heat exchanger 9 where it undergoes a first cooling, then through a second heat exchanger 10, where it undergoes a second cooling, and from where it leaves at a temperature such that after expansion in a reservoir 11 via, for example, a first valve 12 of the Joule-Thomson type, it occurs in said reservoir 11 mainly in a liquid phase which is returned to the underground storage cavity via a second control valve 13 and a pipe 14. The product being in the gas phase in said tank 11 is caused to pass, via a third control valve 15 and a pipe 16, through said first heat exchanger 9 for cooling the compressed gas leaving said compressor 8, before being directed itself towards the inlet of said compressor 8 via a line 17 connected to line 7 to be recycled in the circuit which it has already traversed, until it presents itself in the liquid phase in said reservoir 11.

D'autre part, du produit est prélevé de la phase liquide 3 stockée dans la cavité souterraine 1 par l'intermédiaire d'une canalisation 18 au moyen d'une pompe 19, puis il est surcomprimé par une batterie de pompes 20 jusqu'à une pression telle que le réseau de distribution du produit à l'extérieur puisse être alimenté directement par ladite batterie de pompes après vaporisation, soit à environ 80 bars dans l'exemple de la Figure ci-jointe. Une partie du produit sortant de ladite batterie de pompes 20 est passée dans le deuxième échangeur thermique 10 pour refroidir le gaz comprimé sortant de premier échangeur thermique 9. Dans l'exemple de la Figure ci-jointe, ladite partie du produit sortant de ladite batterie de pompes 20 entre dans le deuxième échangeur thermique 10 à une température voisine de - 150°C et en ressort à environ -80°C. Le débit de produit sortant de ladite batterie de pompes 20 et la proportion de ce produit entrant dans le deuxième échangeur thermique 10 sont réglables au moyen d'une quatrième et d'une cinquième vannes de contrôle 21 et 22 utilisées conjointement, ladite quatrième vanne 21 étant montée en parallèle avec le deuxième échangeur thermique 10 et ladite cinquième vanne 22, montés eux-mêmes successivement en série partant de la sortie de ladite batterie de pompes 20. Les sorties des quatrième et cinquième vannes de contrôle 21 et 22 sont raccordées ensemble sur la sortie générale qui est destinée à être raccordée au réseau de distribution du produit à l'extérieur, après vaporisation.On the other hand, product is withdrawn from the liquid phase 3 stored in the underground cavity 1 by means of a pipe 18 by means of a pump 19, then it is supercharged by a battery of pumps 20 to a pressure such that the distribution network of the product outside can be supplied directly by said battery of pumps after vaporization, that is to say about 80 bars in the example of the attached Figure. Part of the product leaving said pump bank 20 is passed into the second heat exchanger 10 to cool the compressed gas leaving the first heat exchanger 9. In the example of the attached figure, said part of the product leaving said battery of pumps 20 enters the second heat exchanger 10 at a temperature in the region of - 150 ° C and leaves it at approximately -80 ° C. The flow of product leaving said battery of pumps 20 and the proportion of this product entering the second heat exchanger 10 are adjustable by means of a fourth and a fifth control valves 21 and 22 used jointly, said fourth valve 21 being mounted in parallel with the second heat exchanger 10 and said fifth valve 22, themselves mounted successively in series starting from the outlet of said pump bank 20. The outlets of the fourth and fifth control valves 21 and 22 are connected together on the general outlet which is intended to be connected to the product distribution network outside, after spraying.

Les paramètres de fontionnement, tels que les températures, pressions et débits du produit aux différentes étapes du procédé, dépendent, d'une part, de la composition du produit et, d'autre part, des conditions dans lesquelles l'installation, à laquelle est appliquée le procédé de la présente invention, est exploitée.The operating parameters, such as the temperatures, pressures and flow rates of the product at the various stages of the process, depend, on the one hand, on the composition of the product and, on the other hand, on the conditions under which the installation, at which the method of the present invention is applied, is exploited.

On distingue notamment trois types d'installations associés à un stockage souterrain de gaz naturel liquéfié:
- les unités dites d'écrêtement de pointes;
- les terminaux d'exportation;
- les terminaux de réception.There are in particular three types of facilities associated with underground storage of liquefied natural gas:
- so-called tip clipping units;
- export terminals;
- reception terminals.

Une unité d'écrêtement de pointes à laquelle est associée un stockage aérien est exploitée sous la pression atmosphérique et à température de l'ordre de - 160°C. De ce fait, le maintien de la composition du produit peut être assuré par le procédé selon la présente invention.A point clipping unit with which an aerial storage is associated is operated at atmospheric pressure and at a temperature of the order of - 160 ° C. Therefore, the maintenance of the composition of the product can be ensured by the method according to the present invention.

Dans le cas d'un terminal d'exportation, le stockage reçoit le produit stocké par un dispositif de liquéfaction de grande capacité et il est exploité à la pression atmosphérique à environ - 160°C. Le débit nécessaire de phase gazeuse est alors marginal par rapport à celui du remplissage du stockage et son influence sur la composition du produit est négligeable.In the case of an export terminal, the storage receives the product stored by a large capacity liquefaction device and it is operated at atmospheric pressure at approximately - 160 ° C. The required gas phase flow rate is then marginal compared to that of filling the repository and its influence on the composition of the product is negligible.

Dans le cas d'un terminal de réception, le stockage souterrain est expoité à une pression qui peut varier entre la pression atmosphérique et quelques bars mais, en général, les équipements associés ne comprennent pas d'unité de liquéfaction. Par contre, l'installation doit être conçue pour expédier le gas dans le réseau de distribution avec une composition aussi constante que possible. Un dispositif tel que celui de l'exemple décrit en référence à la Figure ci-jointe est applicable à une telle installation.In the case of a reception terminal, the underground storage is operated at a pressure which can vary between atmospheric pressure and a few bars but, in general, the associated equipment does not include a liquefaction unit. On the other hand, the installation must be designed to dispatch the gas in the distribution network with a composition as constant as possible. A device such as that of the example described with reference to the attached Figure is applicable to such an installation.

Claims (3)

1. Procédé pour maintenir constante la composition d'un gaz liquéfié dans un stockage (1) caractérisé en ce qu'il comprend le prélèvement de produit stocké dans la phase gazeuse du stockage (1), sa compression par un compresseur (8), un premier refroidissement, du produit prélevé, dans un premier échangeur thermique (9) suivi d'un deuxième refroidissement dans un deuxième échangeur thermique (10), sa détente dans un réservoir (11) à une température telle, en sortant du deuxième échangeur thermique (10), qu'une partie de produit soit en phase liquide, le retour de ladite phase liquide dans le stockage (1), la phase gazeuse de produit se trouvant dans ledit réservoir (11) étant renvoyée à l'entrée dudit compresseur (8), après être passée dans ledit premier échangeur thermique (9) pour refroidir le produit sortant dudit compresseur (8), le prélèvement en phase liquide (3) de produit stocké depuis ledit stockage (1) par une pompe (19), la surcompression de ladite phase liquide prélevée depuis ledit stockage par une batterie de pompes (20), une partie du produit sortant de ladite batterie de pompes (20) étant passée dans le deuxième échangeur thermique (10) pour refroidir le produit sortant dudit premier échangeur thermique (9) avant de rejoindre le reste du produit sortant de ladite batterie de pompes pour être dirigée ensuite vers le réseau de distribution, après vaporisation.1. Method for keeping constant the composition of a liquefied gas in a storage (1) characterized in that it comprises the withdrawal of product stored in the gas phase of the storage (1), its compression by a compressor (8), a first cooling of the product sampled in a first heat exchanger (9) followed by a second cooling in a second heat exchanger (10), its expansion in a tank (11) at such a temperature, leaving the second heat exchanger (10), that part of the product is in the liquid phase, the return of the said liquid phase to the storage (1), the gaseous phase of the product being in the said reservoir (11) being returned to the inlet of the said compressor ( 8), after having passed through said first heat exchanger (9) to cool the product leaving said compressor (8), the withdrawal in liquid phase (3) of product stored from said storage (1) by a pump (19), the overcompression of said liquid phase taken off uis said storage by a pump bank (20), part of the product leaving said pump bank (20) being passed into the second heat exchanger (10) to cool the product leaving said first heat exchanger (9) before joining the rest of the product leaving said pump bank to then be directed to the distribution network, after vaporization. 2. Procédé selon la revendication 1 caractérisé en ce qu'une vanne de contrôle (12) du type de Joule-Thomson est prévue en amont dudit réservoir (11).2. Method according to claim 1 characterized in that a control valve (12) of the Joule-Thomson type is provided upstream of said tank (11). 3. Procédé selon la revendication 1 ou la revendication 2 caractérisé en ce que la détente de produit dans ledit réservoir (11) est adiabatique.3. Method according to claim 1 or claim 2 characterized in that the expansion of product in said tank (11) is adiabatic.
EP86402321A 1985-10-21 1986-10-16 Process for maintaining the composition of a stored product constant in a low-temperature liquefied gas storage space Expired EP0223669B1 (en)

Applications Claiming Priority (2)

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FR8515562 1985-10-21
FR8515562A FR2588947B1 (en) 1985-10-21 1985-10-21 PROCESS FOR MAINTAINING THE COMPOSITION OF THE CONSTANT STORED PRODUCT IN LOW TEMPERATURE LIQUEFIED GAS STORAGE

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EP0223669A1 true EP0223669A1 (en) 1987-05-27
EP0223669B1 EP0223669B1 (en) 1989-07-26

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EP (1) EP0223669B1 (en)
JP (1) JPH0792198B2 (en)
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EP0223669B1 (en) 1989-07-26
JPS62270900A (en) 1987-11-25
US4689064A (en) 1987-08-25
DE3664616D1 (en) 1989-08-31
FR2588947B1 (en) 1989-02-10
JPH0792198B2 (en) 1995-10-09
FR2588947A1 (en) 1987-04-24

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