EP0223669B1 - 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
EP0223669B1
EP0223669B1 EP86402321A EP86402321A EP0223669B1 EP 0223669 B1 EP0223669 B1 EP 0223669B1 EP 86402321 A EP86402321 A EP 86402321A EP 86402321 A EP86402321 A EP 86402321A EP 0223669 B1 EP0223669 B1 EP 0223669B1
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EP
European Patent Office
Prior art keywords
product
heat exchanger
compressor
leaving
product leaving
Prior art date
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Expired
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EP86402321A
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German (de)
French (fr)
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EP0223669A1 (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 process for : keeping constant the composition of a product like liquefied gas stored at low temperature in a warmer environment.
  • a method for keeping the composition of a product of the liquefied gas type constant comprising successively the evacuation of product from said gas phase, its compression by a compressor, its cooling in heat exchange means, its expansion in a tank at a temperature such as a first quantity of the product leaving said heat exchange means liquefies while a second quantity of the product leaving said heat exchange means remains gaseous and the return of said first quantity liquefied in said storage, said second quantity remained gaseous passing against the current in said heat exchange means to participate said cooling of the product leaving said compressor, is characterized in that said second quantity é remained gaseous is returned to the inlet of said compressor.
  • said heat exchange means consist of at least first and second counter-current heat exchangers; said second quantity remaining gaseous passes only through said first heat exchanger to participate in said cooling of the product leaving said compressor; said method also comprises drawing off using a product pump of said liquid phase, then overcompressing it using a pump battery, part of the product leaving said pump battery being diverted to pass in said second heat exchanger and cooling 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 in vapor form.
  • the method of the invention corresponds to an installation comprising at least two circuits.
  • One which can be called a reliquefaction circuit, carries the gas phase to be evacuated. It features the orga nes necessary for its partial reliquefaction including a compressor and heat exchangers. It is also established in a closed loop.
  • the other for example called the draw-off circuit, makes it possible to extract the liquid phase to bring it to pressure and temperature conditions suitable for the distribution of the product to consumers.
  • 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 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 keeps the storage temperature substantially constant, at a temperature depending on the operating pressure, a temperature which can be of the order of -125 ° C to -160 ° C.
  • the cavity is closed in upper part by a tight plug 6 through which pipes can pass.
  • the product is withdrawn 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 the which is applied the method of the present invention, is exploited.
  • a peak clipping unit with which an aerial storage is associated is operated under 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 around -160 ° C.
  • the required flow rate of the gaseous phase is then marginal by compared to 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.

Description

La présente invention concerne un procédé pour : maintenir constante la composition d'un produit genre gaz liquéfié stocké à basse température dans un milieu plus chaud.The present invention relates to a process for : keeping constant the composition of a product like liquefied gas stored at low temperature in a warmer environment.

Il est intéressant de stocker en particulier les gaz naturels sous forme liquéfiée en raison du moindre volume qu'ils occupent alors. Cela conduit à des stockages à basse température (couramment entre -162°C et -100°C environ) et sous pression. Pour réaliser de telles conditions, on a souvent recours à des stockages souterrains plus sûrs à la fois du point de vue thermique (les roches sont généralement de mauvais conducteurs de la chaleur) et sur le plan de la sécurité (possibilité de confinement en dehors de toute présence de comburant par exemple). Toutefois, le massif rocheux d'accueil transmet à la longue une certaine quantité de chaleur aux produits stockés. La nature de ces derniers fait qu'il s'ensuit une lente évaporation de leur phase liquide. Toutes roches d'accueil confondues, il faut en effet compter avec des taux d'évaporation journaliers de l'ordre de 0,5%.It is advantageous to store in particular natural gases in liquefied form because of the smaller volume which they then occupy. This leads to storage at low temperature (commonly between -162 ° C and -100 ° C approximately) and under pressure. To achieve such conditions, underground storage is often used, both from a thermal point of view (rocks are generally poor conductors of heat) and from a safety point of view (possibility of containment outside any presence of oxidizer for example). However, the receiving rock mass in the long term transmits a certain amount of heat to the stored products. The nature of the latter means that there follows a slow evaporation of their liquid phase. All reception rocks combined, it is indeed necessary to count with daily evaporation rates of the order of 0.5%.

Ce phénomène est gênant à deux titres. Tout d'abord la quantité de vapeur s'accroissant, la pression au sein du stockage risque de s'élever. Pour éviter qu'elle n'atteigne des valeurs insupportables vis-à-vis de la résistance mécanique de l'infrastructure du stockage, on prend donc la précaution d'autoriser quasiment en permanence l'évacuation de la vapeur excédentaire. Comme les produits stockés sont relativement précieux, il ne s'agit pas pour autant de rejeter cette vapeur dans l'atmosphère. Et cela d'autant moins que les quantités intéressées sont importantes si l'on considère la durée de vie de tels stockages (plusieurs dizaines d'années). Aussi s'efforce-t-on plutôt de les réintroduire dans le stockage sous une forme appropriée.This phenomenon is troublesome for two reasons. First of all the quantity of steam increasing, the pressure inside the storage may rise. To prevent it from reaching unbearable values vis-à-vis the mechanical strength of the storage infrastructure, we therefore take the precaution of almost permanently allowing the evacuation of excess steam. As the products stored are relatively precious, this does not mean releasing this vapor into the atmosphere. And all the less since the quantities involved are significant if we consider the lifespan of such storage (several decades). We therefore try rather to reintroduce them into storage in an appropriate form.

Le brevet américain US-A 3 857 245 déposé en 1973 par J.K. Jones enseigne comment y parvenir. La quantité de vapeur évacuée est tout d'abord comprimée, puis elle est refroidie et enfin détendue au sein d'un réservoir de sorte qu'une partie redevient liquide. Ce condensat peut alors être ramené dans le stockage sans y entraîner d'augmentation appréciable de la pression. La partie de produit restée gazeuse au sein du réservoir de détente est, de son côté, envoyée dans un échangeur thermique où elle est à même de refroidir la vapeur évacuée qui vient juste d'être comprimée. Dans ce document antérieur, il est toutefois prévu de rejeter à l'extérieur ce reliquat gazeux.American patent US-A 3,857,245 filed in 1973 by J.K. Jones teaches how to do this. The quantity of vapor evacuated is first compressed, then it is cooled and finally expanded in a tank so that part becomes liquid again. This condensate can then be brought back into storage without causing an appreciable increase in pressure. The portion of product remaining gaseous in the expansion tank is, for its part, sent to a heat exchanger where it is able to cool the evacuated steam which has just been compressed. In this previous document, it is however planned to discharge this gaseous residue to the outside.

Ce dernier aspect de la méthode de Jones rend impossible son application directe aux stockages de gaz liquéfiés. En effet leur taux d'évaporation reste, d'une manière relative, très important. Or, les produits stockés ne sont pas des gaz purs, mais plutôt des mélanges de gaz. Aussi, leur phase liquide et leur phase gazeuse admettent-elles des compositions différentes. On conçoit dès lors que le rejet systématique d'une quantité de vapeur, même réduite par le biais d'une reliquefaction partielle, finisse par aboutir à un changement de la composition des produits stockés.This last aspect of Jones' method makes it impossible to apply it directly to liquefied gas storage. Indeed their rate of evaporation remains, in a relative way, very important. However, the products stored are not pure gases, but rather mixtures of gases. Also, their liquid phase and their gas phase admit different compositions. It is therefore understandable that the systematic rejection of a quantity of vapor, even reduced by means of a partial reliquefaction, ends up leading to a change in the composition of the stored products.

A la vérité, c'est là le second problème posé par l'évaporation dont les stockages de gaz liquéfiés sont le siège. Les produits stockés risquent en effet de voir leur phase liquide s'enrichir petit à petit en gaz plus lourds. A terme, ceux-ci ne seraient alors plus du tout compatibles avec les diverses utilisations auxquelles ils sont destinés. Par exemple, leur pouvoir calorifique en tant que carburants serait modifié dans des proportions telles que les brûleurs ne tarderaient pas à être tout à fait inadaptés. Afin de remédier à ce changement de composition, s'impose d'emblée l'idée de maintenir au sein du système formé par le stockage et les divers conduits à la fois le condensat du réservoir de détente et le reliquat de la vapeur évacuée. Toutefois cela peut être réalisé de multiple façons.In truth, this is the second problem posed by the evaporation which liquefied gas storage is the seat. The stored products may indeed see their liquid phase gradually enriched with heavier gases. Ultimately, these would then no longer be compatible with the various uses for which they are intended. For example, their calorific value as fuels would be changed in such proportions that the burners would soon be completely unsuitable. In order to remedy this change in composition, the idea of maintaining within the system formed by the storage and the various conduits is essential from the start, both the condensate of the expansion tank and the remainder of the evacuated steam. However, this can be done in many ways.

C'est ainsi que la présente invention a pour but de développer un procédé judicieux mettant en oeuvre ce principe. En particuier, le procédé recherché doit aboutir à une installation dont le coût de fonctionnement et de mise en place est minimal.This is how the present invention aims to develop a judicious process implementing this principle. In particular, the process sought must lead to an installation, the cost of operation and installation of which is minimal.

Selon la présente invention, un procédé pour maintenir constante la composition d'un produit du type gaz liquéfié, ledit produit comportant une phase liquide et une phase gazeuse et étant stocké dans un milieu dont la température est supérieure à celle dudit produit, ledit procédé comprenant successivement l'évacuation de produit de ladite phase gazeuse, sa compression par un compresseur, son réfroidissement dans des moyens d'échanges thermiques, sa détente dans un réservoir à une température telle qu'une première quantité du produit sortant desdits moyens d'échanges thermiques se liquéfie tandis qu'une seconde quantité du produit sortant desdits moyens d'échanges thermiques reste gazeuse et le retour de ladite première quantité liquéfiée dans ledit stockage, ladite seconde quantité restée gazeuse passant à contre-courant dans lesdits moyens d'échanges thermiques pour participer audit refroidissement du produit sortant dudit compresseur, est caractérisé en ce que ladite seconde quantité restée gazeuse est renvoyée à l'entrée dudit compresseur.According to the present invention, a method for keeping the composition of a product of the liquefied gas type constant, said product comprising a liquid phase and a gaseous phase and being stored in a medium whose temperature is higher than that of said product, said method comprising successively the evacuation of product from said gas phase, its compression by a compressor, its cooling in heat exchange means, its expansion in a tank at a temperature such as a first quantity of the product leaving said heat exchange means liquefies while a second quantity of the product leaving said heat exchange means remains gaseous and the return of said first quantity liquefied in said storage, said second quantity remained gaseous passing against the current in said heat exchange means to participate said cooling of the product leaving said compressor, is characterized in that said second quantity é remained gaseous is returned to the inlet of said compressor.

De façon avantageuse, lesdits moyens d'échanges thermiques sont constitués par au moins un premier et un second échangeurs thermiques a contre-courant; ladite seconde quantité restée gazeuse passe uniquement dans ledit premier échangeur thermique pour participer audit refroidissement du produit sortant dudit compresseur; ledit procédé comprend par ailleurs le soutirage à l'aide d'une pompe de produit de ladite phase liquide, puis sa surcompression a l'aide d'une batterie de pompes, une partie du produit sortant de ladite batterie de pompes étant dérivée pour passer dans ledit second échangeur thermique et 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 sous forme vapeur.Advantageously, said heat exchange means consist of at least first and second counter-current heat exchangers; said second quantity remaining gaseous passes only through said first heat exchanger to participate in said cooling of the product leaving said compressor; said method also comprises drawing off using a product pump of said liquid phase, then overcompressing it using a pump battery, part of the product leaving said pump battery being diverted to pass in said second heat exchanger and cooling 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 in vapor form.

Comme cela apparaît dans cette brève description, le procédé de l'invention correspond à une installation comprenant au moins deux circuits. L'un qui peut être appelé circuit de reliquéfaction, véhicule la phase gazeuse à évacuer. Il comporte les organes nécessaires à sa reliquéfaction partielle dont un compresseur et des échangeurs thermiques. Il est en outre établi en boucle fermée. L'autre, dénommé par exemple circuit de soutirage, permet d'extraire la phase liquide pour l'amener à des conditions de pression et de température adaptées à la distribution du produit aux consommateurs.As appears in this brief description, the method of the invention corresponds to an installation comprising at least two circuits. One, which can be called a reliquefaction circuit, carries the gas phase to be evacuated. It features the orga nes necessary for its partial reliquefaction including a compressor and heat exchangers. It is also established in a closed loop. The other, for example called the draw-off circuit, makes it possible to extract the liquid phase to bring it to pressure and temperature conditions suitable for the distribution of the product to consumers.

Il est remarquable qu'au sein même du circuit de reliquéfaction, la vapeur restant dans le réservoir de détente est ramenée à l'entrée du compresseur. Cette fraction de vapeur pourrait tout aussi bien être réitroduite dans le stockage lui-même. Mais, pour cela, un tube supplémentaire de communication avec le stockage devrait être prévu. En cas de stockage souterrain, il s'ensuivrait un coût de mise en place du tube et des pertes de charges au sein de ce tube rendant l'installation moins intéressante. Au contraire, la présente disposition optimise son efficacité. En effet, le reliquat de vapeur se trouve à une température inférieure a celle de la phase gazeuse massée au ciel du stockage souterrain. Le compresseur se contente en conséquence d'une puissance d'autant moins importante que la quantité de vapeur froide introduite à son entrée est maximisée.It is remarkable that even within the reliquefaction circuit, the vapor remaining in the expansion tank is brought back to the inlet of the compressor. This vapor fraction could just as easily be re-produced in the repository itself. But, for this, an additional communication tube with the storage should be provided. In the case of underground storage, this would entail a cost of installing the tube and pressure drops within this tube, making the installation less advantageous. On the contrary, this provision optimizes its effectiveness. Indeed, the remainder of vapor is at a temperature lower than that of the gaseous phase massed in the sky of the underground storage. The compressor is therefore content with less power when the quantity of cold steam introduced at its inlet is maximized.

Par ailleurs, on a intérêt à coupler les circuits de reliquéfaction et de soutirage en prévoyant deux échangeurs thermiques, l'un d'eux étant commun aux deux circuits. Ainsi une partie du circuit de soutirage est-elle mise à profit pour participer au refroidissement de la vapeur à reliquéfier. Il s'ensuit certes une augmentation de la température du gaz soutiré. Mais celle-ci est de toute façon nécessaire afin de délivrer aux usagers un gaz sous forme vapeur à la température ambiante. Ainsi l'énergie globale requise est-elle moins importante puisqu'un circuit consomme les calories transportées par l'autre tandis que le second utilise les frigories du premier.Furthermore, it is advantageous to couple the reliquefaction and withdrawal circuits by providing two heat exchangers, one of them being common to the two circuits. Thus, part of the withdrawal circuit is used to participate in the cooling of the vapor to be re-liquefied. This certainly increases the temperature of the gas withdrawn. But this is in any case necessary in order to deliver to the users a gas in vapor form at room temperature. Thus the overall energy required is less important since a circuit consumes the calories transported by the other while the second uses the frigories of the first.

D'autres caractéristiques et avantages de la présente invention apparaîtront mieux à la lecture de la description suivant 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 keeps the storage temperature substantially constant, at a temperature depending on the operating pressure, a temperature which can be of the order of -125 ° C to -160 ° C. The cavity is closed in 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 withdrawn 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 du 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 the which is applied the method of the present invention, 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 peak clipping unit with which an aerial storage is associated is operated under 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 around -160 ° C. The required flow rate of the gaseous phase is then marginal by compared to 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 exploité 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 (4)

1. A method of maintaining constant the composition of a product of the liquefied gas type, said product comprising a liquid phase (3) and a gas phase (4) and being stored in a medium (5) whose temperature is higher than the temperature of said product, said method comprising successively evacuating product in said gas phase (4), compressing it by means of a compressor (8), cooling it in heat exchanger means (9, 10), expanding it in a tank (11) to a temperature such that a first quantity of the product leaving said heat exchanger means (9, 10) liquefies, whereas a second quantity of the product leaving said heat exchanger means (9, 10) remains gaseous, and returning said first liquefied quantity into said store (1), said second quantity that remains gaseous passing as a counterflow through said heat exchanger means (9, 10) in order to participate in said cooling of the product leaving said compressor (8), the method being characterized in that said second quantity that remains gaseous is returned to the inlet of said compressor (8).
2. A method according to claim 1, characterized in that:
said heat exchanger means (9, 10) are constituted by at least first and second quantity that remains gaseous passes solely through
said first heat exchanger (9) in order to participate in said cooling of the product leaving said compressor (8); and in that
said method further includes bleeding the product in the liquid phase (3) by means of a pump, then raising its pressure by means of a battery (20) of pumps, with a portion of the product leaving said battery (20) of pumps being diverted to pass through said second heat exchanger (10) to cool the product leaving said first heat exchanger (9) prior to rejoining the remainder of the product leaving said battery (20) of pumps so as to be subsequently directed towards a network for distribution in the form of vapor.
3. A method according to claim 1 or claim 2, characterized in that a Joule-Thomson type control valve (12) is provided upstream from said tank (11).
4. A method according to any one of claims 1 to 3, characterized in that the expansion of the 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)

Application Number Priority Date Filing Date Title
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 EP0223669A1 (en) 1987-05-27
EP0223669B1 true EP0223669B1 (en) 1989-07-26

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EP (1) EP0223669B1 (en)
JP (1) JPH0792198B2 (en)
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FR (1) FR2588947B1 (en)

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FR2588947A1 (en) 1987-04-24
JPH0792198B2 (en) 1995-10-09
EP0223669A1 (en) 1987-05-27
JPS62270900A (en) 1987-11-25
US4689064A (en) 1987-08-25
FR2588947B1 (en) 1989-02-10
DE3664616D1 (en) 1989-08-31

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