System for storing a gas intended for a tank for transporting and / or storing the gas

Abstract

The invention relates to a system (1) for storing a collected gas in a tank (2) for transporting and / or storing the gas, characterised in that the storage system (1) comprises a main pipe (12) fluidically connecting an upper volume (10) of the tank (2) to a high-pressure storage device (14) for the gas, the main pipe (12) comprising a compression assembly (17) including a first compression device (18) and a second compression device (20) arranged one after the other between the tank (2) and the high-pressure storage device (14) for the gas, the second compression device (20) comprising a plurality of compression stages (201, 202, 203, 204), the storage system (1) comprising a consumption line (25) extending between a point of divergence (26) and at least one consumer (28) of the gas, the point of divergence (26) being situated on the main pipe (12) between the first compression device (18) and the second compression device (20), the storage system (1) comprising at least one heat exchanger (32) through which the consumption line (25) and an exchange portion (34) of the main pipe (12) pass, the exchange portion (34) of the main pipe (12) being situated within the compression assembly (17).

Description

DESCRIPTION Title of the invention: Gas storage system intended for a transport and / or storage tank for said gas.

[0001] The present invention relates to the field of transport and storage of a liquefied gas, for example dihydrogen. It relates more particularly to installations for a sealed and thermally insulated tank for the storage and / or transport of the liquefied gas.

[0002] Liquefied gas is transported by sea in sealed, thermally insulated storage tanks installed on transport vessels. The gas is kept in liquid form to increase the amount transported per tank, as the volume occupied by one kilogram of gas in liquid form is much smaller than the volume occupied by one kilogram of gas in gaseous form. These tanks maintain the liquefied gas at very low temperatures, specifically for dihydrogen, below -250°C, the temperature at which dihydrogen is in liquid form at atmospheric pressure.

[0003] The tank has a sealed wall that defines the storage volume of liquefied gas. This wall is subject to a heat flow that tends to warm the tank's contents, resulting in the evaporation of the liquefied gas. The tank is considered thermally insulating because the structure of its sealed wall is designed to minimize this heat flow and the vaporization of the liquefied gas.

[0004] The liquefied gas is thus present in the tank in a two-phase liquid-vapor equilibrium state. Part of the liquefied gas is in the vapor phase, thus forming an evaporation gas in a larger volume of the tank, while the liquefied gas is mainly in the liquid phase in a smaller volume of the tank.

[0005] It is sought to prevent excessive accumulation of evaporation gas in the tank, as this accumulation has the adverse effect of increasing the pressure within the storage tank and the latter is designed for a maximum pressure of around 2 bar absolute.

[0006] To prevent this excessive accumulation of vaporized gas, several solutions are proposed in the prior art. One of these solutions consists of transferring all or part of the excess vaporized gas to one or more gas consumers, such as propulsion and electrical generation devices or combustion devices capable of producing electricity.

[0007] However, it may happen that the consumption capacity of these consumers is insufficient to absorb all the excess evaporation gas. In this case, it becomes possible to store the unused excess evaporation gas. For this purpose, the excess gas can be directed to storage devices specifically designed for this purpose. High-pressure storage devices, in which the gas is stored under high pressure, can be used to optimize the use of available storage space.

[0008] Before storage, the gas must be compressed to high pressure. However, since the vaporized gas from the tank is at a pressure close to atmospheric pressure, the required compression is substantial. Consequently, particularly energy-intensive compression equipment is essential to achieve this high pressure. This compression also raises the gas temperature, necessitating cooling at the outlet of the compression equipment, particularly to prevent overheating. However, this cooling process results in additional energy consumption.

[0009] The invention falls within this context by proposing a gas storage system for a transport and / or storage tank, allowing the gas to be cooled during its compression, without increasing the energy consumption of the storage system, by using the gas sent to consumers for this cooling.

[0010] The present invention has as its main object a system for storing a gas taken from within a transport and / or storage tank of said gas, characterized in that the storage system comprises a main conduit fluidly connecting a higher volume of the tank to a high-pressure gas storage device.

[0011] The main pipeline includes a compression assembly comprising a first compression device and a second compression device arranged successively between the tank and the high-pressure gas storage device, the second compression device comprising a plurality of compression stages.

[0012] The storage system includes a consumption line extending between a divergence point and at least one consumer of said gas, the divergence point being disposed on the main line between the first compression device and the second compression device, the storage system including at least one heat exchanger extending at a distance from the divergence point and through which passes the consumption line and an exchange portion of the main line, said exchange portion of the main line being disposed within the compression assembly.

[0013] The gas transported and / or stored in the tank may be a gas with a very low boiling point, often at temperatures expressed in negative degrees Celsius, such as hydrogen. During transport and / or storage, this gas is primarily in liquid form within a compartment of the tank. However, heat transfer occurs through a tank wall, which can warm the gas and lead to its partial vaporization.

[0014] It is therefore important to note that inside the tank housing, the gas exists in both liquid and gaseous forms. Due to gravity, the liquid gas remains at the bottom of the housing, referred to as the lower volume of the housing, while the gaseous gas occupies the top of the tank, designated as the upper volume of the housing.

[0015] It is understood that, depending on the quantity of gas in gaseous and liquid form, the lower and upper volumes fluctuate. As will become apparent from the description, the present invention makes it possible to control the pressure rise of the tank, which cannot reach a high pressure (typically a maximum pressure of around 2 bar) through high-pressure storage or gas consumption, while simultaneously limiting the energy consumption associated with managing the temperature of the evaporating gas. In other words, the invention ensures minimal energy consumption for storing the gas in gaseous form.

[0016] The main line, being fluidly connected to the upper volume of the tank, is configured to draw the gas in vapor form from the tank. The gas then flows through at least a portion of the main line.

[0017] It should be understood that, when the first compression device and the second compression device are arranged successively on the main line, this means that, according to a direction of gas flow in the main line from the tank to the high-pressure storage device, the first compression device is upstream of the second compression device.

[0018] After being drawn from the tank, the gas flows through the tank's main pipeline and passes through the first compression unit, where it is compressed for the first time. Then, the gas, or portion of gas, flowing through the main pipeline downstream of the first compression unit is compressed a second time by the second compression unit, and more specifically by the multiple compression stages of the second compression unit.

[0019] The gas compressed by the second compression unit is then conveyed through the main pipeline to the high-pressure storage unit. This high-pressure storage unit stores the vaporized gas from the high-pressure tank. For this purpose, it may include one or more tanks designed to hold high-pressure gas.

[0020] Preferably, the high-pressure storage device is configured to store the gas at a pressure between 200 and 700 bar absolute.

[0021] It should be noted that the vaporized gas drawn from the tank via the main line is not systematically stored. Indeed, the consumption line, which is connected on one side to the main line at the divergence point and on the other side to at least one consumer, allows all or part of the gas circulating in the main line between the first and second compression units to be drawn and delivered to at least one consumer.

[0022] It is thus understood that the consumption line allows the gas compressed by the first compression device to be recovered to meet the needs of at least one consumer.

[0023] It should also be noted that the compression of the first compression device can be adjusted to compress the gas to a pressure acceptable to the consumer(s).

[0024] This compressed gas, drawn from the main pipeline via the consumption line, is then conveyed to at least one consumer. Before reaching this consumer, the gas flowing in the consumption line is heated, some distance from the point of divergence, by passing through at least one heat exchanger in the storage system. The gas flowing in the consumption line is thus able to absorb heat and therefore serves as a source of cooling within the heat exchanger. It is clear that the fact that the heat exchanger extends some distance from the point of divergence allows for a clear distinction between the gas flowing in the consumption line and the gas flowing in the main pipeline, and ensures that they have distinct thermal properties, thus making heat exchange beneficial.

[0025] This heat exchanger comprises at least two passes: a first pass formed by the consumption line which passes through said heat exchanger and therefore serves as a source of cold, and a second pass formed by the exchange part of the main pipe.

[0026] The heat exchange section of the main pipe is a portion of said pipe positioned within the compression assembly. More precisely, this heat exchange section can be located, for example, between the first compression device and the second compression device, or between two compression stages among the plurality of compression stages constituting the second compression device.

[0027] Located within the compression assembly, the heat exchanger section of the main pipeline forms part of that pipeline through which the gas flows in compressed form. For example, when the heat exchanger section is positioned between two compression stages, the gas flows at the pressure corresponding to the compression level defined by the first compression stage through which the gas passes.

[0028] It should be noted that, due to compression within the compression unit, the gas circulating in the heat exchange section of the main pipeline is heated. It is therefore necessary to cool it to prevent an excessive temperature rise, given that the compression unit compresses the gas to very high pressures. Advantageously, the invention achieves this cooling by performing a heat exchange between the compressed gas in the heat exchange section and the cold gas circulating in the consumption line and destined for at least one consumer, thereby reducing the energy consumption of the compression unit, and in particular of the second compression device.

[0029] To be cooled, the heat exchange section of the main pipe passes through the heat exchanger. The gas flowing through this section may have been compressed by at least one compression stage of the secondary compression unit, particularly when this section is located between two compression stages of said unit. Conversely, the gas flowing in the consumption line has not been subjected to this compression by this stage. Consequently, the gas in the heat exchange section is hotter than the gas in the consumption line.

[0030] The gas flowing in the supply line is thus able to absorb heat and acts as a cooling source within the heat exchanger, while due to compression, the gas in the heat exchange section of the main line is heated and can therefore release heat. As a result, during heat exchange within the heat exchanger, the gas in the heat exchange section of the main line is cooled by the gas flowing in the supply line, which consequently heats up.

[0031] The heat exchanger as defined in the invention, that is, an exchanger arranged at a distance from a point of divergence between a consumption line and a main line, and therefore a heat exchanger configured to exchange heat between gas flowing in the consumption line and gas flowing in the main line, thus prevents an excessive rise in the temperature of the gas in the main line due to compression, while consuming little energy, since the heat exchanger uses the cold already present in the storage system, in this case, the cold of the gas flowing in the consumption line. The use of this heat exchanger within the storage system therefore eliminates the need for external coolers to cool the gas during compression, thereby reducing the overall energy consumption of the storage system.

[0032] It should also be noted that this heat exchanger makes it possible to lower the temperature of the gas circulating in the main line to levels lower than those achievable with external coolers, such as water or air coolers.

[0033] Furthermore, by cooling the gas after at least one of the compression stages of the second compression device, the invention makes it possible to reduce the temperature of the gas before it enters the next compression stage, which facilitates the compression process and thus leads to a reduction in energy consumption.

[0034] In addition to preventing temperature rise, the heat generated by compression is also used to warm the gas circulating in the consumption line, thus avoiding the use of an external heater and achieving further energy savings.

[0035] A storage system according to the invention, comprising such a heat exchanger, thus makes it possible to reduce energy consumption by at least 20% compared to a system not incorporating this invention. By way of non-limiting example and to illustrate this energy saving, compressing dihydrogen to 300 bar, without the use of the present invention, results in energy consumption in the form of electricity of 1.84 kWh / kg of H2, whereas by using the storage system according to the invention, energy consumption in the form of electricity is reduced to 1.44 kWh / kg of H2.

[0036] Such a heat exchanger also allows the gas temperature to be lowered than that achieved by an external cooler. As a result, the gas can be stored at a lower temperature within the high-pressure storage unit. Storing the gas at a lower temperature thus increases the gas density for the same pressure. In other words, at the same pressure, a larger quantity of gas can be stored in the high-pressure storage unit.

[0037] According to an optional feature of the invention, the exchange part is arranged between two compression stages of the plurality of compression stages of the second compression device.

[0038] The gas circulating in the exchange section is therefore a gas that has been compressed by one of the compression stages. This gas is thus at a pressure corresponding to that defined by the compression stage that compressed the gas.

[0039] Conversely, the gas flowing in the consumption line is at a lower pressure, corresponding to that of the first compression stage (or that of the expansion valve when the consumption line includes one). Consequently, the gas in the heat exchanger, having undergone greater compression, is at a higher temperature than the gas flowing in the consumption line.

[0040] Thus, the gas from the consumption line acts as a source of cold, while the gas circulating in the exchange part serves as a source of heat. The heat exchanger therefore allows the gas circulating in the main pipe to be cooled after its compression, using the cold of the gas from the consumption line.

[0041] It should be noted that the invention also covers embodiments where the storage system includes several heat exchangers. For example, the storage system includes a heat exchanger cooling the gas flowing in the main line after its compression by the first compression device, and other heat exchangers cooling the gas flowing in the main line at each compression stage of the second compression device.

[0042] According to an optional feature of the invention, the storage system includes a heat exchanger through which passes an initial portion of the main line and a final portion of the main line, the initial portion of the main line being disposed between the tank and the first compression device, the final portion of the main line being disposed between the second compression device and the high-pressure storage device.

[0043] This heat exchanger can be integrated into any embodiment of the present invention.

[0044] Unlike a heat exchanger, a heat exchanger is not designed to limit the temperature increase caused by gas compression within the main pipeline prior to subsequent compression, and therefore does not limit the energy consumption generated by that compression. Instead, the heat exchanger is designed to cool the gas to a low temperature before it is stored at high pressure.

[0045] Storing gas at high pressure and low temperature increases its density. For example, the density of dihydrogen is 20 kg / m³. 3 at room temperature, while at -200°C and an absolute pressure of 275 bar, it reaches 60 kg / m³ 3 .

[0046] Increasing the density of high-pressure gas allows for increased storage capacity within the same volume of the high-pressure storage device. Thus, by cooling the high-pressure compressed gas, it is possible to store a greater quantity of gas compared to an uncooled gas.

[0047] Furthermore, for an equivalent amount of stored gas, this allows for a reduction in the pressure required for storage. In other words, it is possible to decrease the compression needed to store a given quantity of gas, which reduces the compression effort at the second compression stage, thus saving energy.

[0048] The heat exchanger is a two-pass exchanger, with a first pass formed by the initial portion of the main pipe, and a second pass formed by the final portion of the main pipe.

[0049] Positioned between the tank and the first compression device, the gas circulating in the initial section comes directly from the tank before being compressed by the first compression device. Upon entering the heat exchanger, the gas circulating in the initial section is therefore at a very low temperature, close to its storage temperature in the tank, for example, between -245 and -230 °C. Due to this low temperature, the gas circulating in the initial section is able to absorb heat and thus serves as a cooling source within the heat exchanger.

[0050] Located between the second compression stage and the high-pressure storage unit, the gas circulating in the final section has been repeatedly compressed by the first and second compression stages. Consequently, even if this gas has undergone one or more heat exchanges through the heat exchanger(s), the gas circulating in the final section is capable of releasing heat within the heat exchanger. For example, upon entering the heat exchanger, the gas in the final section may be at a temperature between 5 and 43 °C.

[0051] Therefore, the gas circulating in the initial section cools the gas circulating in the final section via the heat exchanger. This heat transfer results in a decrease in the gas temperature within the final section, the value of which at the heat exchanger outlet can, for example, be between -244 and -220 °C.

[0052] According to an optional feature of the invention, the storage system comprises at least two heat exchangers, each of the at least two heat exchangers being arranged between two compression stages.

[0053] According to an optional feature of the invention, the storage system comprises at least two heat exchangers, each of the at least two heat exchangers being arranged between two successive compression stages.

[0054] In other words, the storage system includes at least one first heat exchanger positioned between two successive compression stages of the second compression device, and a second heat exchanger positioned between two other successive compression stages of said second compression device.

[0055] The expression "successive compression stages" refers to two compression stages arranged consecutively, that is to say that the gas flowing in the main pipe is first compressed by one of the two compression stages, then immediately by the second, with optional cooling via a heat exchanger, without undergoing intermediate compression by another compression stage.

[0056] It should be noted that the fact that the heat exchangers are arranged between two successive compression stages does not limit the invention to the presence of a heat exchanger between each compression stage. Indeed, it is conceivable that, for example, for four compression stages, the storage system could have only two heat exchangers.

[0057] In cases where multiple heat exchangers are installed within the storage system, the main pipe comprises a number of heat exchanger sections equal to the number of heat exchangers. For example, the first heat exchanger section might pass through the first heat exchanger, while the second heat exchanger section passes through the second heat exchanger. The first heat exchanger section then corresponds to a portion of the main pipe located between two successive compression stages, and the second heat exchanger section to another portion of the main pipe, located between two other successive compression stages.

[0058] Each heat exchanger includes, in addition to the pass formed by the heat exchange sections of the main pipe, another pass formed by the consumption line. Thus, in the example described above, a first heat exchange section of the consumption line forms the second pass of the first heat exchanger, while a second heat exchange section of the consumption line forms the second pass of the second heat exchanger.

[0059] It should be noted that the storage system may include more than two heat exchangers. In this case, each heat exchanger is associated with a heat exchange section of the consumption line and a heat exchange section of the main pipe, these latter forming the passes of each heat exchanger respectively.

[0060] According to an optional feature of the invention, the storage system includes a bypass line associated with at least one heat exchanger of the storage system, the bypass line extending between two successive compression stages between which the associated heat exchanger is disposed, the bypass line being disposed in parallel with said associated heat exchanger.

[0061] It is therefore important to understand that at least one of the heat exchangers is associated with a bypass line, so the storage system includes at least one bypass line. Alternatively, each heat exchanger can be associated with a bypass line, in which case the storage system includes multiple bypass lines.

[0062] A bypass line is associated with a heat exchanger, in that the bypass line allows the gas flowing within the main pipe to bypass said heat exchanger by passing through the bypass line.

[0063] For this purpose, the bypass line extends between the two successive compression stages, between which the associated heat exchanger is placed, so as to form a parallel fluidic circuit.

[0064] The term "parallel fluid circuit" should be understood to mean that the bypass line allows the gas to circulate in parallel, either within the heat exchanger associated with the bypass line or within the bypass line itself. The bypass line thus allows the gas to take several paths simultaneously and / or selectively, namely, passing through the heat exchanger and / or through the bypass line.

[0065] According to an optional feature of the invention, the storage system includes at least one cooling means disposed on the bypass line.

[0066] The cooling method uses a cold source external to the storage system.

[0067] According to an optional feature of the invention, the cooling means is a water exchanger, or a seawater exchanger, or a glycol water exchanger.

[0068] The cooling method therefore uses a circulation of water, seawater or glycol water in order to lower the temperature of the gas circulating in the bypass line.

[0069] The gas flowing in the main line can be forced to pass through the bypass line instead of the heat exchanger. This can be done, for example, when the gas in the supply line has already been heated by initial heat exchange and the heat exchanger is not efficient enough to adequately cool the gas in the main line. In this case, the gas is directed to the bypass line, where it can be cooled by the cooling system.

[0070] In this way, it is then possible to efficiently cool the gas during its compression, regardless of the performance of the heat exchanger.

[0071] According to an optional feature of the invention, the storage system includes a destocking line fluidly connecting the high-pressure storage device to at least one consumer.

[0072] This gas extraction line allows the gas stored at high pressure in the high-pressure storage unit to be drawn and delivered to at least one consumer. For this purpose, the extraction line can be directly connected on one side to the high-pressure storage unit and on the other side to at least one consumer. consumer.

[0073] The gas release line may include a pressure-reducing valve. This valve reduces the pressure of the gas coming from the high-pressure storage unit to a level suitable for consumer needs. Furthermore, the pressure-reducing valve regulates the gas flow in the release line, thus controlling the amount of gas transferred from the high-pressure storage unit to at least one consumer.

[0074] Alternatively, the destocking line can also be connected to the main line upstream of the high-pressure storage device and to the consumption line upstream of at least one consumer, in order to destock the gas contained in the high-pressure storage device and convey it to at least one consumer.

[0075] The invention also relates to a method of controlling a storage system as described in this document, in which a quantity of gas stored in the high-pressure storage device is regulated according to a consumption capacity of at least one consumer and according to a quantity of gas in vapor form present in the tank.

[0076] Indeed, when the amount of gas in vapor form in the tank is too high, the excess vaporized gas is vented from the tank to prevent excessive pressure inside. The vaporized gas is then vented through the main pipeline and routed either to at least one consumer, to the high-pressure storage system, or to both, particularly when at least one consumer is unable to use all the gas extracted from the tank.

[0077] According to an optional feature of the invention, the temperature of the gas sent to the high-pressure storage device is a function of the amount of gas flowing in the main line and in the consumption line.

[0078] It is important to note that the more gas the consumption line draws from the main line, the less gas the main line contains downstream of the divergence point. Consequently, the amount of gas decreases in the heat exchanger section of the main line, which forms one of the passes of the heat exchanger, while the amount of gas in the consumption line, constituting the other pass and the heat exchanger's cooling source, increases. This dynamic reduces the amount of gas to be cooled and increases the availability of the cooling source in the heat exchanger, thereby improving the efficiency of gas cooling within the heat exchanger section of the main line.

[0079] Conversely, when the consumption line draws less gas from the main line, the amount of gas in the main line increases downstream of the divergence point. In this case, the amount of gas increases in the heat exchange section of the main line, while the consumption line contains less gas. This situation leads to an increase in the amount of gas to be cooled and a decrease in the available cooling source in the heat exchanger, which may necessitate additional cooling of the gas flowing to storage, for example, at the outlet of the second compression stage.

[0080] According to an optional feature of the invention, the temperature of the gas sent to the high-pressure storage device is regulated by a cooling element disposed on the main line between the compression assembly and the high-pressure storage device.

[0081] In other words, the storage system includes a cooling element located on the main pipeline, downstream of the compression assembly and upstream of the high-pressure storage device. This cooling element may, by way of example but not limitation, use water, seawater, or glycol water as the cooling fluid.

[0082] By being located between the compression unit and the high-pressure storage device, the cooling element helps to lower the temperature at the outlet of the compression unit and thus to regulate the temperature of the gas before it is sent to the high-pressure storage device.

[0083] Other features, details and advantages of the invention will become clearer upon reading the following description on the one hand, and the illustrative and non-limiting examples of embodiments given with reference to the accompanying drawings on the other hand, in which:

[0084] [Fig. 1] is a schematic representation of a first embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas;

[0085] [Fig. 2] is a schematic representation of a second embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas;

[0086] [Fig. 3] is a schematic representation of a third embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas;

[0087] [Fig. 4] is a schematic representation of a fourth embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas.

[0088] The features and variants of the invention can be combined in various ways, provided they are not incompatible or mutually exclusive. In particular, variants of the invention may be conceived comprising only a selection of the features described below, isolated from the other described features, if this selection of features is sufficient to confer a technical advantage and / or to differentiate the invention from the prior art.

[0089] In the figures, elements common to several figures retain the same reference.

[0090] Figure 1 is a schematic representation of a first embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas.

[0091] The gas can be of any type existing in gaseous, liquid, or supercritical form. Dihydrogen is particularly preferred as the gas for storage system 1 according to the invention. This storage system 1 allows for storage at a lower energy cost, even for a gas requiring a very low liquefaction temperature, such as dihydrogen. Other applications for the tank 2, for example with liquefied natural gas, are nevertheless conceivable.

[0092] It should be noted that the invention also covers the case of several tanks 2 mounted in parallel, with a storage system 1 for all the tanks 2 mounted in parallel or a storage system 1 for each tank 2.

[0093] Tank 2 includes a wall 4 which defines a compartment 6. It should be understood that compartment 6 corresponds to an internal void space within tank 2, intended to contain the gas. Wall 4 therefore serves to form this internal void space by defining compartment 6.

[0094] Within this dwelling 6, the gas can be present in different states. It is originally stored in tank 2 in liquid form, but due to a heat flow at the wall 4 which tends to cause the evaporation of the gas, the gas is present in dwelling 6 in both liquid and gaseous form.

[0095] The dwelling 6 thus comprises a lower volume 8, where the gas is in liquid form, and an upper volume 10, where the gas is in gaseous form. Indeed, under the effect of gravity, the gas in liquid form naturally remains in the lower volume 8, which can be considered the lower part of the dwelling 6. At the same time, the gas in gaseous form occupies the part of the dwelling 6 not filled by the liquid gas and therefore naturally remains in the upper volume 10, which can be considered the upper part of the dwelling 6.

[0096] The dimensions, and in particular the height of each volume, vary according to the quantity of gas in liquid form and therefore the additional quantity of gas in vapor form.

[0097] The gas in liquid form is loaded or unloaded into the tank 2 via one or more loading and / or unloading lines 11 of said gas.

[0098] The storage system 1 is installed on said tank 2, more specifically so as to be in fluidic communication with the upper volume 10 of the housing 6 of tank 2. The storage system 1 is thus able to draw gas in the form of vapor from the upper volume 10 of the housing 6 of tank 2.

[0099] The storage system 1 includes in particular a main line 12. This main line 12 extends between the tank 2 and a high-pressure gas storage device 14.

[0100] It should be noted that in order to facilitate reading, in Figure 1 and in the following figures, the main pipe 12 is represented in bolder lines than the other lines through which the gas flows.

[0101] The main line 12 includes more particularly a gas extraction end 16, which is positioned in the upper volume 10 of the housing 6 of the tank 2 in order to be able to draw off the vapor gas contained in said upper volume 10 of the housing 6 of the tank 2. The gas can then flow within the main line 12, in particular from the extraction end 16 to the high-pressure storage device 14.

[0102] The high-pressure storage device 14 is therefore a device for storing the evaporation gas from tank 2 at high pressure. To this end, the high-pressure storage device 14 may include one or more tanks adapted to contain a gas at high pressure. More specifically, the high-pressure storage device 14 may be capable of storing the evaporation gas at a pressure between 200 and 700 bar absolute.

[0103] The storage system 1 also includes a compression unit 17, used in particular to compress the gas flowing in the main line 12, in order to allow high-pressure storage of the evaporation gas from the tank 2. The compression assembly 17 includes, for this purpose, a plurality of compression devices.

[0104] More specifically, the compression assembly 17 comprises a first compression device 18 and a second compression device 20, arranged successively on the main line 12. By "arranged successively", it is meant that the first compression device 18 is the compression device, of these two devices, which is placed closest to the tank 2 and furthest from the high-pressure storage device 14 if one considers the distance traveled by the gas within the main line 12, while the second compression device 20 is the compression device, of these two devices, placed closest to the high-pressure storage device 14 and furthest from the tank 2.

[0105] In other words, when the storage system 1 is in operation, the gas can flow from the extraction end 16 to the high-pressure storage device 14. This means that, following the direction of gas flow in the main pipe 12, the first compression device 18 is upstream of the second compression device 20, and the latter is therefore downstream of the first compression device 18.

[0106] The first compression device 18 is thus configured to compress the gas flowing in the main line 12. When the gas flows from the tank 2 to the first compression device 18, it is at a pressure between 1 and 2.5 bar absolute, generally at atmospheric pressure. The first compression device 18 is thus configured to compress this gas, in order to increase its initial pressure from 1 to 2.5 bar absolute to a final pressure between 5 and 15 bar absolute, for example, around 7 bar absolute.

[0107] The first compression device 18 comprises, in this embodiment, at least one compression stage 181 for compressing the gas flowing in the main conduit 12, this at least one compression stage 181 being the element or one of the elements of the first compression device 18 that enables the compression of the gas. Alternatively, the first compression device 18 could comprise a plurality of compression stages.

[0108] The second compression device 20, located downstream of the first compression device 18 if we consider the direction of gas flow within the main pipe, is therefore configured to compress the gas which has already been compressed by the first compression device 18.

[0109] The second compression device 20 comprises a plurality of compression stages, and more particularly at least two compression stages. In this embodiment, the second compression device 20 comprises a first compression stage 201, a second compression stage 202, a third compression stage 203, and a fourth compression stage 204. Each of these compression stages is designed to compress the evaporation gas to different pressures.

[0110] The first compression stage 201, the second compression stage 202, the third compression stage 203 and the fourth compression stage 204 are arranged successively on the main line 12. By "successively", it should be understood that, according to a direction of gas flow in the main line 12, from the reservoir 2 to the high-pressure storage device 14, the gas first encounters the first compression stage 201 of the second compression device 20, then the second compression stage 202 of the second compression device 20, then the third compression stage 203 of the second compression device 20, and finally the fourth compression stage 204 of the second compression device 20.

[0111] The second compression device 20 is configured to compress the evaporation gas from a pressure between 5 and 15 absolute bars to a pressure between 200 and 700 absolute bars.

[0112] It should be noted that, depending on the type of gas stored in the tank, the compression stages of the second compression unit can be configured to compress the gas to different pressures. For example, when the gas stored in the tank is hydrogen, one of the compression stages of the second compression unit can be preferably configured to compress the gas to a pressure between 20 and 50 bar absolute. Conversely, when the gas stored in the tank is liquefied natural gas (LNG), one of the compression stages of the second compression unit can be advantageously configured to compress the gas to a pressure between 30 and 70 bar absolute.

[0113] It should be noted that the configurations of each compression device and each compression stage are given here by way of example, without being limiting of the invention, provided that their arrangement in relation to each other, as well as the resulting connection and branch points, and the differences in gas pressure within the main conduit 12, conform to what is described elsewhere.

[0114] Between the first compression device 18 and the second compression device 20, the storage system 1 includes a connection point for a consumption line 24, configured to draw gas flowing in the main line 12.

[0115] The consumption line 24 extends from this connection point, called the divergence point 26, located on the main line 12 between the first compression unit 18 and the second compression unit 20, to at least one consumer 28 of this gas. This consumer or these consumers 28 may include any technology using this gas as an energy source. They may also be burners intended to remove excess gas from the tank 2 to produce electricity.

[0116] The gas flow rate in the consumption line 24 is regulated by a control valve 30, which can be either an on / off valve or a proportional valve. An on / off valve alternates between an open and a closed position, while a proportional valve allows for an intermediate position to be selected to adjust the gas flow rate. By regulating the gas flow rate in the consumption line 24, the quantity of gas drawn from the main line 12 to supply the consumption line 24 is controlled, this quantity of gas being adjusted according to the needs of the consumer(s) 28.

[0117] It should be noted that, since the divergence point 26 is located between the first compression device 18 and the second compression device 20, the gas drawn from the consumption line 24 is at a pressure between 5 and 15 absolute bars, which corresponds to the pressure required for the consumer(s) 28.

[0118] It should also be noted that the temperature of the gas drawn from the consumption line 24 is between -210 and -130 °C.

[0119] The storage system 1 is equipped with at least one heat exchanger 32, arranged within the storage system 1 in order to allow heat exchange between the different parts of the storage system 1 where the gas circulates.

[0120] This heat exchanger 32 is specifically configured to allow heat exchange between the consumption line 24 and the main line 12, in order to recover the cold from the gas circulating in the consumption line 24 and thus cool the gas during its compression in the main line 12.

[0121] For this purpose, at least one heat exchanger 32 extends over the consumption line, i.e. at a non-zero distance from the divergence point 26, and the consumption line 24 and a heat exchange portion 34 of the main pipe 12 pass within the at least one heat exchanger 32. The heat exchanger 32 comprises a first pass formed by the consumption line 24, at a distance from the divergence point 26, and a second pass formed by the heat exchange portion 34 of the main pipe 12, these two passes being configured to perform a heat exchange between them.

[0122] The exchange portion 34 of the main pipe 12 which passes within at least one heat exchanger 32 is disposed within the compression assembly 17. More particularly, the exchange portion 34 of the main pipe 12 is disposed between two compression stages of the plurality of compression stages of the second compression device 20 as illustrated by way of example in one of the figures 1 to 4.

[0123] It follows that, by being arranged in this way, at least one heat exchanger 32 makes it possible to carry out a heat exchange by recovering the cold from the gas circulating in the consumption line 24, in order to cool the gas circulating in the exchange part 34 of the main line 12. More particularly, the heat exchanger 32 makes it possible either to cool the gas after its compression by the first compression device 18 when the exchange part 34 is arranged between the first compression device 18 and the second compression device 20, or the gas after its compression by one of the compression stages of the second compression device 20 when the exchange part 34 is arranged between two compression stages of the plurality of compression stages of the second compression device 20.

[0124] In the first embodiment, the storage system 1 includes a first heat exchanger 321, a second heat exchanger 322 and a third heat exchanger 323.

[0125] Within the first heat exchanger 321 passes a first exchange section 361 of the consumption line 24, and a first exchange part 341 of the main line 12. In other words, the first heat exchanger 321 comprises two passes, with the first exchange section 361 of the consumption line 24 which constitutes a first pass of the first heat exchanger 321, and the first exchange part 341 of the main line 12 which constitutes a second pass of the first heat exchanger 321.

[0126] The first exchange section 341 of the main line 12 is located between the first compression stage 201 of the second compression device 20 and the second compression stage 202 of the second compression device 20. The first exchange section 361 of the consumption line 24 is located between the divergence point 26 and at least one consumer 28, i.e. at a distance from the divergence point 26 and at a distance from the consumer 28.

[0127] Thanks to this arrangement of the first exchange part 341 of the main line 12 and the first exchange section 361 of the consumption line 24, a heat exchange occurs within the first heat exchanger 321 between the gas from the divergence point 26, intended for at least one consumer 28 and flowing in the consumption line 24, and the gas flowing between the first compression stage 201 and the second compression stage 202 of the second compression device 20, namely the gas compressed by the first compression stage 201.

[0128] More specifically, the gas circulating in the consumption line 24 is at a first temperature, defined by its compression by the first compression device 18. The gas circulating in the first exchange part 341 is at a second temperature, higher than the first temperature previously mentioned, due to successive compressions, in the first compression device 18 and in the first compression stage 201 of the second compression device 20.

[0129] It follows that the gas circulating in the first exchange section 361 of the consumption line 24 therefore serves as a source of cold to cool the gas circulating in the first exchange part 341 of the main line 12.

[0130] The second heat exchanger 322 also includes two passes: a first pass formed by a second exchange section 362 of the consumption line 24 and a second pass formed by a second exchange part 342 of the main line 12.

[0131] The second exchange section 342 of the main line 12 is positioned between the second compression stage 202 of the second compression device 20 and the third stage of said second compression device 20. The second exchange section 362 of the consumption line 24, for its part, is located between the first exchange section 361 of the consumption line 24 and at least one consumer 28 of the storage system 1.

[0132] A heat exchange thus occurs within the second heat exchanger 322 between the gas circulating in the second exchange section 362 of the consumption line 24 which serves as a source of cold and the gas circulating in the second exchange part 342 of the main line 12 which is then cooled.

[0133] The gas flowing in the second heat exchange section 362 of the consumption line 24 exits the first heat exchanger 321 and therefore has a higher temperature than its temperature before passing through the first heat exchanger 321. The number of frigories it is likely to release is less than in the first heat exchange section 362 of the consumption line 24, but sufficient here to cool the gas flowing in the second heat exchange section 342 of the second heat exchanger 322. Indeed, the gas at the inlet of the second heat exchange section 342 has a higher temperature than the gas at the inlet of the first heat exchange section 341, because the second compression stage 202 is configured to compress the gas more strongly than the first compression stage 201.

[0134] Regarding the third heat exchanger 323, a third exchange section 363 of the consumption line 24 and a third exchange part 343 of the main line 12 pass within said third heat exchanger 323. In other words, the third heat exchanger 323 is also a two-pass exchanger, with a first pass formed by the third exchange section 363 of the consumption line 24, and a second exchange pass formed by the third exchange part 343 of the main line 12.

[0135] The third exchange section 343 of the main line 12 is disposed between the third compression stage 203 of the second compression device 20 and the fourth compression stage 204 of said second compression device 20, while the third exchange section 363 of the consumption line 24 is located between the second exchange section 362 of the consumption line 24 and at least one consumer 28 of the storage system 1.

[0136] Similar to what occurs in the other heat exchangers 32, the gas flowing in the consumption line 24 is heated only by its passage through the first compression device 18 and by the recovery of heat via the previously passed heat exchangers 32. In contrast, the gas flowing in the exchange section 34 has a higher temperature due to its passage through multiple compression devices and compression stages. Consequently, heat exchange occurs in the third heat exchanger 323 between the gas flowing in the third exchange section 363 of the consumption line 24, which acts as a source of cooling, and the gas flowing in the third exchange section 343 of the main line 12, which is then cooled.

[0137] The gas flowing in the third exchange section 363 of the consumption line 24 corresponds to the gas flowing in the consumption line 24 after passing through the first heat exchanger 321 and the second heat exchanger 322. The gas flowing in the third exchange section 343 of the main line 12 corresponds, for its part, to the gas after its compression by the third compression stage 203 of the second compression device 20.

[0138] It follows from this arrangement of the storage system 1 that the evaporation gas is drawn from the tank 2 via the main line 12, then circulates within said main line 12 before being compressed by the first compression device 18. A first fraction of the compressed gas can then be drawn off by the consumption line 24, while a second fraction of the compressed gas can continue its circulation in the main line 12.

[0139] The first portion of the gas flows through the consumption line 24, initially passing through the first heat exchanger 321 via the first heat exchanger section 361, where it acts as a cooling source and recovers heat. This first portion of the gas then continues its path through the second heat exchanger 322 via the second heat exchanger section 362 of the consumption line 24, where it also acts as a cooling source to recover heat. The first portion of the gas then flows through the third heat exchanger 323 via the third heat exchanger section 363 of the consumption line 24, again acting as a cooling source, before reaching at least one consumer 28.

[0140] The second gas fraction flows through the main pipe 12 and is compressed for the first time by the first compression stage 201, which raises its temperature. This second gas fraction then passes into the first heat exchanger 321 via the first exchange section 341, where it is cooled by the gas flowing in the first exchange section 361 of the consumption line 24.

[0141] The second gas fraction is then compressed a second time by the second compression stage 202 of the second compression device 20, resulting in a further increase in its temperature. Subsequently, the second gas fraction passes through the second heat exchanger 322 via the second exchange section 342, where it is cooled by the gas circulating in the second exchange section 362 of the consumption line 24.

[0142] The second gas fraction is compressed again by the third compression stage 203 of the second compression device 20, resulting in a further increase in its temperature. The second gas fraction is then cooled by the gas flowing through the third heat exchanger section 363 of the consumption line 24, passing through the third heat exchanger 323 via the third heat exchanger section 343.

[0143] The second gas fraction is then compressed by the fourth compression stage 204 of the second compression device 20, and then continues its circulation in the main line 12 to the high-pressure storage device 14.

[0144] The arrangement of the heat exchangers 32, as described above, allows the cold of the first gas fraction to be efficiently used to cool the gas flowing in the main line 12 during its compression by the compression unit 17. Using the cold already present in the storage system 1 thus significantly reduces the overall energy consumption of the storage system 1 by lowering the gas temperature prior to compression, thereby reducing the energy required for compression and avoiding the need for external cooling sources. Furthermore, the arrangement of the heat exchangers 32 allows the heat generated by the compression of the second gas fraction flowing in the main line 12 by the second compression unit 20 to be used to reheat the first gas fraction to a temperature suitable for at least one consumer 28.

[0145] Figure 2 is a schematic representation of a second embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas.

[0146] This second embodiment is similar to the first embodiment, but differs in that the storage system 1 includes, in addition to at least one heat exchanger 32, a heat exchanger 38.

[0147] The heat exchanger 38 is configured to recover the cold from the gas flowing in the main line 12 at the outlet of the tank 2, in particular that flowing between the tank 2 and the first compression device 18, in order to use it to cool the gas intended to be stored in the high-pressure storage device 14. More specifically, the heat exchanger 38 cools the gas flowing in the main line 12 between the second compression device 20 and the high-pressure storage device 14.

[0148] For this purpose, the heat exchanger 38 is a two-pass exchanger, with a first pass formed by an initial portion 40 of the main pipe 12 and a second pass formed by a final portion 42 of the main pipe 12.

[0149] The initial portion 40 of the main line 12 is located between the tank 2 and the first compression device 18. In this initial portion 40, the circulating gas is the gas drawn from the tank 2 by the main line 12 before its compression by the first compression device 18. The gas is therefore at a pressure between 1 and 2.5 bar absolute and at a temperature between -245 and -230 °C before passing through the heat exchanger 38.

[0150] The final section 42 of the main pipeline 12 is located between the second compression unit 20 and the high-pressure storage unit 14. Consequently, in this final section 42, the circulating gas is the gas from the second compression unit 20, which is therefore compressed to a pressure between 200 and 700 bar absolute. The temperature of this gas is between 5 and 43 °C before it passes through the heat exchanger 38, resulting from the fact that the gas has been compressed several times and has undergone several prior heat exchanges.

[0151] The gas flowing in the final section 42 of the main pipe 12 is capable of releasing heat, while the gas flowing in the initial section 40 is capable of absorbing heat. The gas flowing in the initial section 40 therefore serves as a source of cooling for the heat exchanger 38.

[0152] As a result, at the outlet of the heat exchanger 38, in other words, after the heat exchange, the gas circulating in the initial portion 40 of the main pipe 12 is then at a temperature between -245 and 42 °C, while the gas circulating in the final portion 42 of the main pipe 12 is then at a temperature between -244 and -220 °C.

[0153] Thanks to this heat exchanger 38, the cold gas drawn from tank 2 is used to cool the high-pressure gas before storage. This results in a gas that is not only at high pressure but also at low temperature in the final section 42 of the main line 12 exiting the heat exchanger 38, thus significantly increasing the quantity of gas that can be stored at high pressure in the high-pressure storage unit 14.

[0154] Taking dihydrogen as the example of the gas stored in tank 2, the use of heat exchanger 38 increases the density of hydrogen at equivalent pressure and thus increases the quantity of gas stored. Indeed, at ambient temperature, the density of hydrogen at 300 bar is approximately 20 kg / m³ 3 Whereas if hydrogen is stored at 300 bar and -200 °C, its density increases to approximately 60 kg / m³ 3 This allows for the storage of a much larger quantity of gas.

[0155] Furthermore, this approach reduces storage pressure for an equivalent density. For example, only 57 bar is needed to achieve a density of 20 kg / m³ 3 , which considerably reduces the energy consumption of the second compression device 20.

[0156] Thus, by compressing the gas less in the second compression device 20, a storage capacity equivalent to that obtained by compressing the gas more without cooling is achieved. The energy consumption of the storage system 1 is therefore reduced.

[0157] It should be noted that the heat exchanger 38 can be used in any embodiment of the invention and is therefore compatible with all embodiments of the invention.

[0158] Figure 3 is a schematic representation of a third embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas.

[0159] This third embodiment is similar to the first embodiment, but differs in that the storage system 1 includes at least one bypass line 44, here a bypass line 44 in the illustrated mode.

[0160] The bypass line 44 is associated with one of the heat exchangers 32 described previously. In other words, in this embodiment, at least one of the three heat exchangers 32 is associated with a bypass line 44. In this embodiment, only the third heat exchanger 323 is associated with a bypass line 44.

[0161] Alternatively, it is conceivable that the first heat exchanger 321 and / or the second heat exchanger 322 be associated with a bypass line 44. It is also possible that each of the heat exchangers 32 be associated with its own bypass line 44.

[0162] The bypass line 44 extends between two successive compression stages, between which the associated heat exchanger 32 is located. Thus, in this embodiment, the bypass line 44 extends between the third compression stage 203 of the second compression device 20 and the fourth compression stage 204 of said second compression device 20.

[0163] The bypass line 44 is arranged in parallel with the heat exchanger 32 associated with it, and more particularly, in this embodiment, the bypass line 44 is arranged in parallel with the third heat exchanger 323.

[0164] By "arranged in parallel", it should be understood that the bypass line 44 allows the parallel circulation of the gas, either in the third heat exchanger 323 via the third exchange part 343 of the main line 12, or in the bypass line 44. In other words, the bypass line 44 allows the gas to take several paths simultaneously and / or selectively, namely the passage through the third heat exchanger 323 or the passage through the bypass line 44.

[0165] More specifically, bypass line 44 extends between a first junction 46 and a second junction 48, these two junctions ensuring the fluid connection between bypass line 44 and the main conduit 12.

[0166] The first junction 46 is located between the third compression stage 203 and the third heat exchanger 323, while the second junction 48 is located between the third heat exchanger 323 and the fourth compression stage 204.

[0167] Thus, after being compressed by the third compression stage 203, the gas reaches the first junction 46 and can then:

[0168] - circulate through the third heat exchanger 323 via the third exchange part 343 of the main pipe 12,

[0169] - take the bypass line 44 to directly reach the second junction 48 without passing through the third heat exchanger 323, where it is reinjected into the main pipe 12 before being compressed by the fourth compression stage 204 of the second compression device 20,

[0170] - to divide into two flows, a first flow passing through the third heat exchanger 323 and a second flow passing through the bypass line 44.

[0171] It should be noted that, in order to regulate the amount of gas taken from the bypass line 44, the storage system 1 includes a first control valve positioned on the bypass line 44 and a second control valve positioned on the main line 12, between the first junction 46 and the third heat exchanger 323.

[0172] Alternatively, a three-way valve can be installed at the first junction 46 to regulate the amount of gas taken from the bypass line 44.

[0173] A cooling means 50 is arranged on the bypass line 44, this cooling means 50 being configured to cool the gas circulating in said bypass line 44. For this purpose, the cooling means 50 can be a water cooler, in which water circulates to exchange heat and thus cool the gas circulating in the bypass line 44. Alternatively, the cooler can also use seawater or glycol water.

[0174] As a result, when the gas is diverted to bypass the third heat exchanger 323, the gas passes through the bypass line 44 and is then cooled by this cooling means 50.

[0175] Therefore, the gas is cooled after its compression by the third compression stage 203, even when the third heat exchanger 323 is no longer able to cool it sufficiently, since the gas then passes through the bypass line 44 and is cooled by the cooling means 50.

[0176] Such a situation, where the third heat exchanger 323 is unable to cool the gas sufficiently, occurs for example when the gas circulating in the third exchange section 363 of the main line 12 is insufficiently cold, in particular due to excessive heating due to its prior passage through the first heat exchanger 321 and the second heat exchanger 322.

[0177] In this embodiment, the storage system 1 also includes a cooling element 52 installed on the main line 12. This cooling element 52 is a water cooler, and it is configured to lower the temperature of the gas flowing in the main line 12 by using water as the cooling fluid.

[0178] The cooling element 52 is arranged on the main line 12, between the second compression device 20 and the high-pressure storage device 14. In other words, according to the direction of gas flow, the cooling element 52 is downstream of the second compression device 20, and more particularly, downstream of the fourth compression stage 204 of the second compression device 20. The cooling element 52 is therefore configured to cool the gas after its compression by the fourth compression stage 204 of the second compression device 20.

[0179] Figure 4 is a schematic representation of a fourth embodiment of a gas storage system 1 installed on a tank 2 for transporting and / or storing said gas.

[0180] This fourth embodiment is similar to the first embodiment, but is distinguished by the integration of a destocking line 54 within the storage system 1.

[0181] The destocking line 54 is configured to allow the destocking of gas stored in the high-pressure storage device 14, and more specifically to convey this gas to at least one consumer 28.

[0182] For this purpose, the destocking line 54 fluidly connects the high-pressure storage device 14 to at least one consumer 28. More specifically, the destocking line 54 extends between a first branch 56 and a second branch 58. The first branch 56 is directly connected to the high-pressure storage device 14, while the second branch 58 is directly connected to at least one consumer 28.

[0183] The gas release line 54 also includes a pressure-reducing valve 60, configured both to reduce the pressure of the gas flowing in said gas release line 54 and to control the gas flow rate. Thus, the pressure-reducing valve 60 regulates the quantity of gas drawn from the high-pressure storage device 14 and delivered to the consumer 28, while simultaneously lowering the gas pressure to a level compatible with the needs of said consumer 28.

[0184] It should be noted that, alternatively, the first branch 56 could be arranged on the main line 12, between the second compression device 20 and the high-pressure storage device 14 and that the second branch 58 could be arranged on the consumption line 24.

[0185] The invention also relates to a method of controlling the storage system 1. In this method, the quantity of gas stored within the high-pressure storage device 14 is regulated according to several factors.

[0186] A first factor is the consumption capacity of the consumer(s) 28, and a second factor is the quantity of gas in the form of vapor present in the tank 2.

[0187] Indeed, when the quantity of gas in vapor form (BOG) becomes too high in tank 2, it becomes necessary to vent it to avoid excessive pressure. The gas in vapor form is therefore vented, notably through the main line 12, and can be consumed by the consumer(s) 28. However, when the consumer(s) 28 are unable to consume all of the gas in vapor form, the high-pressure storage device 14 takes over and stores this gas. Consequently, the quantity of gas stored in the high-pressure storage device 14 depends on the consumption capacity of the consumer(s) 28 as well as the presence of excess gas in vapor form within the tank 2.

[0188] The process according to the invention also makes it possible to control the temperature of the gas sent to the high-pressure storage device 14 since the quantity of gas circulating in the exchange section of the consumption line 24 and in the exchange part 34 of the main line 12 within each heat exchanger 32 influences the cooling performance of this heat exchanger 32 and therefore the final temperature of the gas at the outlet of the compression devices 18, 20.

[0189] In order to control the quantity of gas circulating in the exchange section of the consumption line 24 and in the exchange part 34 of the main line 12, and thus adjust the cooling performance of at least one heat exchanger 32, it is possible to control the withdrawal of gas circulating in the main line 12 by the consumption line 24 by means of the regulating valve 30.

[0190] For example, when the supply line 24 draws a large quantity of gas from the main line 12, a greater quantity of gas flows through the heat exchange section of the supply line 24, thus providing an increased source of cooling. Conversely, less gas flows through the heat exchange section 34 of the main line 12. Consequently, when the supply line 24 draws a large quantity of gas, the cooling of the gas flowing through the heat exchange section 34 of the main line 12 is very efficient.

[0191] Conversely, when the consumption line 24 draws a smaller quantity of gas, the cold source in the exchange section of the consumption line 24 is less important, while more gas flows in the exchange section 34 of the main line 12. This results in less efficient cooling of the gas flowing in the exchange section 34 of the main line 12.

[0192] Furthermore, the method according to the invention makes it possible to regulate the temperature of the gas sent to the high-pressure storage device 14 using the bypass line 44. Indeed, this bypass line 44 offers the possibility of bypassing one or more heat exchangers 32, depending on the number and arrangement of the bypass line(s) within the storage system 1. It then becomes possible to control the passage of the gas either within at least one heat exchanger 32, or within the bypass line 44, which therefore makes it possible to regulate the temperature of the gas.

[0193] As described above, the present invention effectively achieves its stated objectives, namely reducing the energy consumption associated with compressing evaporation gas from a tank for storage at high pressure, and increasing the storage capacity of this gas under high pressure. To this end, the invention proposes a storage system for storing evaporation gas at high pressure, the evaporation gas being cooled during its compression by at least one heat exchanger using the evaporation gas dedicated to at least one consumer of said storage system as its cooling source.

[0194] The present invention is not limited to the means and configurations described and illustrated herein, and also extends to any equivalent means and configuration, as well as any technically operative combination of such means.

Claims

DEMANDS:

1. A gas storage system (1) for gas taken from a tank (2) for transporting and / or storing said gas, characterized in that the storage system (1) comprises a main line (12) fluidly connecting an upper volume (10) of the tank (2) to a high-pressure storage device (14) for the gas, said main line (12) comprising a compression assembly (17) including a first compression device (18) and a second compression device (20) arranged successively between the tank (2) and the high-pressure storage device (14) for the gas, the second compression device (20) comprising a plurality of compression stages (201, 202, 203, 204), the storage system (1) comprising a consumption line (24) extending between a divergence point (26) and at least one consumer (28) of said gas,the divergence point (26) being disposed on the main line (12) between the first compression device (18) and the second compression device (20), the storage system (1) comprising at least one heat exchanger (32) arranged at a distance from the divergence point (26) and through which passes the consumption line (24) and a heat exchange portion (34) of the main line (12), said heat exchange portion (34) of the main line (12) being disposed within the compression assembly (17).

2. A storage system (1) according to claim 1, wherein the exchange portion (34) is disposed between two compression stages of the plurality of compression stages (201, 202, 203, 204) of the second compression device (20).

3. A storage system (1) according to any one of claims 1 or 2, comprising a heat exchanger (38) through which pass an initial portion (40) of the main line (12) and a final portion (42) of the main line (12), the initial portion (40) of the main line (12) being disposed between the tank (2) and the first compression device (18), the final portion (42) of the main line (12) being disposed between the second compression device (20) and the high-pressure storage device (14).

4. Storage system (1) according to any one of claims 1 to 3, comprising at least two heat exchangers (32), each of the at least two heat exchangers (32) being disposed between two compression stages.

5. Storage system (1) according to any one of claims 1 to 4, comprising a bypass line (44) associated with at least one heat exchanger (323) of the storage system (1), the bypass line (44) extending between two successive compression stages (203, 204) between which the associated heat exchanger (323) is disposed, the bypass line (44) being disposed in parallel with said associated heat exchanger (323).

6. Storage system (1) according to claim 5, comprising at least one cooling means (50) disposed on the bypass line (44).

7. Storage system (1) according to claim 6, wherein the cooling means (50) is a water, seawater, or glycol-water heat exchanger.

8. Storage system (1) according to any one of claims 1 to 7, wherein the high-pressure storage device (14) is configured to store the gas at a pressure between 200 and 700 bar absolute.

9. Storage system (1) according to any one of claims 1 to 8, comprising a destocking line fluidly connecting the high-pressure storage device (14) to at least one consumer (28).

10. Method for controlling a storage system (1) according to any one of claims 1 to 9, wherein a quantity of gas stored in the high-pressure storage device (14) is regulated according to a consumption capacity of at least one consumer (28) and according to a quantity of gas in vapor form present in the tank (2) 11. Control method according to claim 10, characterized in that the temperature of the gas sent to the high-pressure storage device (14) is a function of the quantity of gas flowing in the main line (12) and in the consumption line (24).

12. Control method according to any one of claims 10 or 11 in combination with claim 6 or 7, characterized in that the temperature of the gas sent to the high-pressure storage device (14) is regulated by a cooling element (52) disposed on the main line (12) between the compression assembly (17) and the high-pressure storage device (14).

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