Method for cooling a heat exchanger of a gas supply system for a gas-consuming device of a ship

Abstract

The invention relates to a method for supplying gas to a gas-consuming device (101) arranged on board a ship comprising a tank (200) containing liquid and gaseous gas, the method comprising at least: a supply step of supplying, by means of a supply unit (110), to the gas-consuming device (101), gas extracted in gaseous state from the tank (200), a condensation step of condensing at least a portion of the gas extracted in gaseous state from the tank (200) by means of a condensation unit (120) comprising at least one heat exchanger (121) configured to exchange heat between the extracted gas between the supply unit (110) and the gas-consuming device (101) and the gas flowing between the tank (200) and the supply unit (110), the method being characterized in that it comprises a step of cooling the heat exchanger (121), the cooling step being implemented before the condensation step and at least partially simultaneously with the supply step.

Description

Technical Field

[0001] This invention relates to the field of ships, whose propulsion engines are powered by natural gas, and whose ships enable the carrying and / or transport of liquefied natural gas. Background Technology

[0002] Such ships typically include tanks containing liquefied natural gas. Natural gas is liquid at atmospheric pressure and temperatures below -160°C. These tanks are never fully insulated, so at least some of the natural gas evaporates within them. Therefore, these tanks contain both liquefied and gaseous natural gas. This gaseous natural gas forms the top of the tank, and the pressure within this top must be controlled to prevent damage to the tank. In a known manner, the natural gas, present in at least a portion of its gaseous form within the tank, is thus used to power the ship's propulsion engines, etc.

[0003] Nevertheless, when the ship is stationary, the natural gas consumption of these engines is zero, or nearly zero, and the gaseous natural gas in the tanks is no longer consumed by these engines. Therefore, a reliquefaction system is implemented on board, which enables the condensation of the evaporated natural gas present in the tanks so that it can be returned to the tanks in a liquid state.

[0004] Current reliquefaction systems require the fabrication of energy-intensive units. In practice, the system temperature, particularly the temperature of the heat exchanger used to process the gas, must be kept below a threshold value at which reliquefaction can begin. It should be understood that this delay increases the time required to bring the reliquefaction system into operation, and this delay is also a particularly energy-intensive period. This invention falls within this context by providing a method for supplying gas to a gas-consuming device, which includes a condensation unit responsible for liquefying the gas, at least one heat exchanger of which is cooled to reduce the operating time of the condensation unit. Summary of the Invention

[0005] Therefore, one object of the present invention relates to a method for supplying gas to a gas-consuming device on a ship, the gas-consuming device comprising a tank containing liquid and gaseous gases, the method comprising at least:

[0006] -The supply step of supplying gas extracted in gaseous form from the tank to the gas-consuming equipment via the supply unit.

[0007] - A condensation step involving condensing at least a portion of the gas extracted from the tank in a gaseous state by means of a condensation unit, the condensation unit including at least one heat exchanger configured to exchange heat between the extracted gas between the supply unit and the gas consumption device and the gas flowing between the tank and the supply unit, the method being characterized in that it includes a cooling step of cooling the heat exchanger, the cooling step being performed prior to the condensation step and at least partially simultaneously with the supply step.

[0008] Compared to existing technologies, this method allows gas to flow within a heat exchanger even when the gas-consuming device consumes the available vapor-state gas in the top space of the tank. This flow is controlled and is particularly low compared to the flow rates of the rest of the system, thus preventing imbalance in the latter.

[0009] This design allows for cooling, and in particular maintaining, the heat exchanger at low temperatures, close to the operating conditions during its condensation step. Consequently, the energy consumption and / or uptime of the condensation unit are significantly reduced, enabling the maximization of liquefied gas volume and thus minimizing its losses.

[0010] According to one feature of the invention, the cooling step includes controlling the flow rate of the gas flowing through the first channel of the heat exchanger to between 2% and 12% of the flow rate of the gas extracted in a gaseous state from the tank during the supply step. For example, when the flow rate of the gas in a vapor state leaving the tank is 2500 kg / h, the flow rate of the gas cooling the heat exchanger is between 50 kg / h and 300 kg / h.

[0011] According to another feature of the invention, the cooling step includes controlling the flow rate of gas flowing through the second channel of the heat exchanger during the cooling step to a ratio between 75% and 135% relative to the flow rate of gas flowing through the first channel of the heat exchanger. Preferably, this ratio is equal to 115%, which ensures optimal cooling. This ratio has the effect of controlling the heat exchange between the two channels of the heat exchanger to avoid generating thermal stresses that could damage the heat exchanger. Therefore, the use of aluminum plate heat exchanger technology is feasible and much cheaper than existing technologies.

[0012] According to one feature of the method, the cooling step includes controlling the flow rate of the gas flowing through the first channel of the heat exchanger during the cooling step to between 50 kg / h and 300 kg / h. These flow rate values ​​ensure that the cooling step does not negatively affect the gas supply step to the gas consumer, while ensuring that only a negligible portion of the gas flow rate delivered to the consumer is extracted, and that the heat exchanger is set or maintained at a low temperature to enable rapid operation of the condensing unit.

[0013] It should be noted that the gas flow rate through the first channel of the heat exchanger during the cooling step is 3% to 20% of the gas flow rate through the first channel of the heat exchanger during the condensation step. This allows for the distinction between the cooling and condensation steps.

[0014] Advantageously, the gas flowing through the first channel of the heat exchanger during the cooling step is added to the supply unit. Thus, the gas that has cooled the heat exchanger is mixed with the gas from the tank and sent to the supply unit.

[0015] According to one characteristic, the cooling step of a heat exchanger is the step of cooling the heat exchanger so that the heat exchanger temperature drops from a positive degree Celsius temperature to a negative degree Celsius temperature. For example, the temperature of the heat exchanger ranges from +42 degrees Celsius to -117 degrees Celsius, especially maintaining a maximum temperature difference of 27 degrees Celsius between the first and second channels.

[0016] According to another feature, the cooling step of the heat exchanger is a step of maintaining the heat exchanger at a cool temperature, causing the heat exchanger to change from a first negative Celsius temperature to a second negative Celsius temperature. According to one example, the first temperature can be equal to the second temperature, resulting in the heat exchanger being maintained at a temperature of, for example, -120 degrees Celsius, so that the latter can be immediately used to implement the condensation step. According to another example, the first temperature is higher than the second temperature, for example, -117 degrees Celsius, and the second temperature is for example -120 degrees Celsius.

[0017] It should be noted that the cold holding step precedes the condensation step. In other words, the cold holding step occurs sequentially between the two condensation steps. This choice is advantageous for keeping the heat exchanger cold because the cold holding step begins when the exchanger is at a very low temperature and ends at the end of the condensation phase.

[0018] The present invention also relates to a system for supplying gas to at least one gas consuming device, the system comprising at least:

[0019] Tanks for storing and / or transporting liquid and gaseous gases, the tanks being used to contain gases.

[0020] A supply unit for gas-consuming equipment, configured to extract gas from a tank and increase its pressure to supply the gas-consuming equipment.

[0021] A condensation unit includes at least one heat exchanger, the heat exchanger including a first channel and a second channel. The condensation unit is configured such that extracted gas flowing between a supply unit and a gas consumption device flows through the first channel, while gas flowing between the tank and the supply unit flows through the second channel.

[0022] An apparatus for cooling a heat exchanger includes at least one control element and means for controlling the temperature of the heat exchanger, the control element being configured to control the flow rate of gas flowing through a first channel.

[0023] Based on the corresponding flow directions of the gas in the first and second channels of the heat exchanger, the first channel is arranged between the tank and the supply unit, and the second channel is arranged between the supply unit and the tank.

[0024] According to one embodiment of the invention, a control member regulates the flow rate through the first channel. For example, the flow control member may be in the form of a valve adapted to have at least one open position, a closed position, and multiple intermediate positions, which allows the flow rate of gas intended to supply the heat exchanger to be controlled, at least during the cooling step.

[0025] Based on a characteristic of this system, the control component is configured to maintain the gas flow rate through the first channel between 50 kg / h and 300 kg / h. Therefore, this control component is designed to precisely control the gas flow rate within the pipeline, but this flow rate is significantly lower than the flow rate used in the condensation step when the system is in liquefaction mode.

[0026] According to a feature of the invention, the means for controlling the temperature of the heat exchanger includes at least one bypass conduit for bypassing a second channel of the heat exchanger. Therefore, the flow rate of gas flowing through the second channel can be controlled relative to the gas flow rate through the bypass conduit, thereby affecting the heat exchange occurring between the first and second channels of the heat exchanger.

[0027] According to another feature, the means for controlling the temperature of the heat exchanger includes at least one component for controlling the gas flow rate through a bypass duct, the gas flow rate through the bypass duct depending at least on the gas temperature determined at the inlet of the first channel of the heat exchanger. In other words, the at least one bypass duct extends between the tank and the supply unit, and is connected in parallel with the second channel of the heat exchanger.

[0028] As a supplement, the gas flow rate through the bypass duct depends on the gas temperature determined at the outlet of the second channel of the heat exchanger.

[0029] These arrangements are designed to control the temperature of the gas flowing through the first and second channels to avoid any mechanical stress caused by excessive temperature difference between the first and second channels of the heat exchanger.

[0030] According to one aspect of the invention, the condensing unit includes at least a heat exchanger, hereinafter referred to as a first heat exchanger, which includes a first channel and a second channel. The condensing unit also includes a second heat exchanger, which is the site for heat exchange between gas extracted in liquid form from the tank and gas from the first channel of the first heat exchanger.

[0031] The first heat exchanger is the heat exchanger described above, namely a heat exchanger including a first channel and a second channel. The condensation unit is configured such that the extracted gas between the supply unit and the gas consumption device flows through the first channel, while the gas flowing between the tank and the supply unit flows through the second channel.

[0032] The second heat exchanger is located downstream of the first heat exchanger relative to the extraction airflow between the supply unit and the consumption equipment. Based on the same airflow direction, the second heat exchanger is arranged upstream of the cooling device.

[0033] According to one aspect of the system, the supply unit includes at least one temperature raising section for raising the temperature of gas extracted from the tank in liquid form, and at least one pressure raising section for raising the gas pressure to supply gas consuming equipment.

[0034] To increase the gas pressure for supplying the gas-consuming device, the supply unit includes at least one compression member. Advantageously, the supply unit may include two compression members to ensure redundancy, i.e., if one of the two compression members fails, the other compression member can replace it. According to the invention, the supply unit is configured to increase the gas pressure to a pressure appropriate to the needs of the gas-consuming device. For example, the gas pressure may be between 1 bar and 400 bar, advantageously between 1 bar and 17 bar, and more advantageously between 6 bar and 17 bar.

[0035] According to the features of this embodiment, the temperature rise section of the supply unit may include, for example, at least one heat exchanger and at least one compression device, the compression device being disposed between the heat exchanger and the gas pressure rise section, the heat exchanger including at least one first line and at least one second line, the first line being supplied with gas extracted in liquid form from the tank, the second line being supplied with gas extracted in liquid form from the tank, and at least one expansion device being arranged between the tank and the first line of the heat exchanger.

[0036] According to this embodiment, the temperature rise section thus forms a gas evaporation section, that is, the liquid gas extracted from the tank is heated and thus turns into a gaseous state before entering the pressure rise section of the supply unit.

[0037] The present invention also relates to a liquefied gas transport vessel, comprising at least one gas supply system according to any one of the above features, wherein the vessel carries tanks, supply units, condensation units and cooling devices.

[0038] The present invention also relates to a system for loading or unloading liquefied gas, the system combining at least one land or port facility and at least one ship for transporting liquefied gas as described above.

[0039] Finally, the present invention relates to a method for loading or unloading liquefied gas on a gas carrier as described above, wherein the liquefied gas is transported via pipeline from a floating or onshore storage facility to a tank on the ship or from a tank on the ship to a floating or onshore storage facility. Attached Figure Description

[0040] On the one hand, other features, details, and advantages of the invention will become clearer through reading the following description, and on the other hand, through the examples provided. These examples are for illustrative purposes only and are not intended to limit the invention to the accompanying drawings, in which:

[0041] [ Figure 1 The schematic diagram illustrates the gas supply system of the gas consumption device according to the present invention;

[0042] [ Figure 2 ]Illustrative illustration Figure 1 The first embodiment of the gas supply system shown;

[0043] [ Figure 3 This schematically illustrates the temperature holding mode. Figure 2 Implementation method of the gas supply system shown;

[0044] [ Figure 4 This schematically illustrates the condensation mode. Figure 2 Implementation method of the gas supply system shown;

[0045] [ Figure 5 A second embodiment of the gas supply system according to the present invention is illustrated schematically;

[0046] [ Figure 6 This schematically illustrates the temperature holding mode. Figure 5 Implementation method of the gas supply system shown;

[0047] [ Figure 7 This schematically illustrates the condensation mode. Figure 5 Implementation method of the gas supply system shown;

[0048] [ Figure 8 [A cross-sectional schematic diagram of an LNG tanker and a dock used for loading and / or unloading the tanker.] Detailed Implementation

[0049] In the remainder of the specification, the terms "upstream" and "downstream" should be understood according to the direction of flow of liquid, gas, or two-phase gas through the element under consideration. Figure 3 , 4 In Figures 6 and 7, dashed lines represent loop conduits in which no gas flows, while solid lines represent loop conduits in which gas flows, regardless of the state of the gas. Furthermore, the thickness of the lines is proportional to the flow rate of the gas flowing in the respective conduit. Thus, the thinnest lines represent conduits in which gas flows at a first flow rate between 50 kg / h and 300 kg / h, while thicker lines represent conduits in which gas flows at a second flow rate strictly higher than 300 kg / h.

[0050] In this document, the terms “liquefaction” and “condensation” are used indiscriminately.

[0051] Figures 1 to 7 A gas supply system 100 for at least one gas consuming device 101 is shown. As shown, the system 100 includes at least one tank 200 containing gas for supplying to at least one gas consuming device 101, the gas being contained in both liquid and gaseous states within the tank 200. In the following description, the space of the tank 200 occupied by the gaseous gas is referred to as the "top space 201" and the space of the tank 200 occupied by the liquid gas is referred to as the "bottom space 202".

[0052] The following description provides a specific example of the application of the invention, wherein tank 200 contains natural gas. It should be understood that this is merely an example of application, and the gas supply system 100 according to the invention can be used for different types of gases, such as hydrocarbons or hydrogen. Similarly, the accompanying drawings illustrate a system for supplying gas to one or two fuel-consuming devices; however, it should be understood that the system can be adapted to supply more than two gas-consuming devices without departing from the scope of the invention. In the remainder of the specification, unless otherwise stated, the term "gas-consuming device" refers to one or more gas-consuming devices.

[0053] therefore, Figure 1 The main schematic illustration shows the gas supply system 100 of the gas consuming device 101 when it stops, that is, when there is no gas (whether in a gaseous, liquid or two-phase state) flow.

[0054] According to the present invention, the system 100 includes at least the aforementioned tank 200, a supply unit 110 of at least one gas consuming device 101, a gas condensation unit 120, the gas consuming device 101, and a cooling device 130.

[0055] As shown in the figure, at least first conduits 102, 102' are disposed between the tank 200 and the supply unit 110. According to the invention, the supply unit 110 can be supplied with gas extracted in a gaseous state from the top space 201 of the tank or with gas extracted in a liquid state from the tank 200. In other words, the first conduit 102' can extend between the top space 201 of the tank and the supply unit 110, or the first conduit 102 can extend between the bottom of the tank 202 and the supply unit 110, more specifically, between the pump 300 disposed in the bottom of the tank 202 and the supply unit 110.

[0056] Regardless of the state of the gas supplied to the supply unit 110, the supply unit 110 includes at least one temperature-raising section 111 configured to increase the temperature of the gas extracted from the tank 200, so that the gas exits the supply unit 110 in a gaseous state and at a temperature appropriate to the needs of the gas-consuming device 101. The supply unit 110 also includes at least one pressure-raising section 112 configured to increase the pressure of the gas to a pressure appropriate to the needs of the gas-consuming device 101. As described below, the temperature-raising section 111 includes at least one heat exchanger, and the pressure-raising section 112 includes at least one compression member.

[0057] System 100 includes at least one second conduit 103 that connects supply unit 110 to gas consumption device 101. As should be understood from the foregoing, gaseous gas having a temperature and pressure adapted to the needs of gas consumption device 101 flows through the second conduit 103.

[0058] According to the present invention, the pressure-increasing portion 112 includes at least one compression member 118, for example... Figures 2 to 7 As shown, the compression member 118 is configured to increase the gas pressure therethrough to a pressure that meets the requirements of the gas consuming device 101. According to any embodiment described below, the pressure increasing unit 112 more specifically includes a first compression member 118 and a second compression member 118' mounted in parallel with each other.

[0059] According to different application examples of the present invention, only the first compression member 118 can be configured to operate, while the second compression member 118' is ensured to be redundant, i.e., the second compression member 118' can replace the first compression member in the event of a failure of the first compression member 118. Alternatively, the first compression member 118 and the second compression member 118' can be configured to operate simultaneously, i.e., a first portion of the gas from the pressure rise section 111 is compressed by the first compression member 118, and a second portion of the gas is compressed by the second compression member 118', wherein the first and second portions of the gas are different. Each of these compression members 118, 118' is also connected to a second conduit 103, which itself is connected to the gas consumption device 101.

[0060] According to any of these application examples, gas is introduced into the first compression member 118 and / or the second compression member 118' in a gaseous state and at a pressure of approximately 1 bar, and exits the first compression member 118 and / or the second compression member 118' in a gaseous state and at high pressure, i.e., pressure between 1 bar and 400 bar, advantageously between 1 bar and 17 bar, and more advantageously between 6 bar and 17 bar. The compression level at the outlet of the first compression member 118 and / or the second compression member 118' is parameterized according to the type of gas consumption device 101 to be supplied.

[0061] The condensation unit 120 includes at least one heat exchanger 121 adapted to exchange heat between the extract gas between the supply unit 110 and the gas consumption device 101 and the gas flowing between the tank 200 and the supply unit 110. More specifically, the heat exchanger 121 includes at least one first channel 122 and at least one second channel 123, the first channel 122 being supplied with the extract gas between the supply unit 110 and the gas consumption device 101, i.e., the gas compressed by the pressure riser section 112, and the second channel 123 being supplied with the gas flowing between the tank top space 201 and the pressure riser section 112 of the supply unit 110.

[0062] Advantageously, when the aforementioned heat exchanger 121 is referred to as the first heat exchanger, the condensation unit 120 includes another heat exchanger, hereinafter referred to as the second heat exchanger 145. During the condensation step, the second heat exchanger 145 functions as a condenser. The second heat exchanger 145 includes a first channel 146 and a second channel 147, through which extracted gas between the supply unit 110 and the gas consumption device 101 flows, and through which gas extracted in liquid form from the tank 200 flows.

[0063] The first channel 146 of the second heat exchanger 145 is located downstream of the first channel 122 of the first heat exchanger 121. The second channel 147 of the second heat exchanger 145 is arranged upstream of the supply unit 110.

[0064] The second heat exchanger 145 is a heat exchange site between the liquid gas with a temperature of at most -163°C and the extracted gas at the outlet of the supply unit 110. The extracted gas can be at a positive temperature after entering the first channel 122 of the first heat exchanger 121.

[0065] The first heat exchanger 121 associated with the second heat exchanger 145 constitutes one embodiment of the condensation unit 120.

[0066] In the following description, the heat exchanger is the first heat exchanger mentioned above.

[0067] As shown in the figure, at least one third conduit 104 extends between the tank top space 201 and the second channel 123 of the heat exchanger 121, and at least one fourth conduit 105 extends between the second conduit 103 and the first channel 122, in particular the fourth conduit 105 extends between the first connection point 401 located on the second conduit 103 and the inlet of the first channel 122 of the heat exchanger 121.

[0068] In addition, the first channel 122 is connected to the bottom of the tank 202 via the pipe 143, and the second channel 123 is connected to the supply unit 110 via the ninth conduit 136 and the sixth conduit 107.

[0069] The heat exchanger 121 of the condensation unit 120 is configured to exchange heat between gaseous gas extracted from the tank top space 201 and extracted gas downstream of the supply unit 110 (i.e., gaseous gas whose temperature and pressure are adapted to the needs of the gas consumption device 101). In other words, the heat exchanger 121 is configured to exchange heat between gas extracted in gaseous form from the tank top space 201 and directly fed into the heat exchanger 121, and gas extracted in gaseous form from the tank top space 201 whose pressure has been increased by the pressure increase portion 112 of the supply unit 110. By “directly fed into the heat exchanger 121,” it should be understood that the gaseous natural gas does not undergo any pressure or temperature change before being fed into the heat exchanger 121, and in particular the second passage 123 of the heat exchanger 110, except for changes related to its flow in the conduit under consideration.

[0070] The result of this heat exchange is at least that the gas flowing in the first channel 122 of the heat exchanger 121 is cooled, and the temperature of the gas flowing in the second channel 123 of the heat exchanger 121 is increased.

[0071] According to the invention, the cooling device 130 of the heat exchanger 121 includes at least one control member 131 for controlling the airflow flowing in the first channel 122 of the heat exchanger 121. The cooling device 130 also includes at least one phase separator 133 having a two-phase inlet connected to the outlet of the first channel 122, a gas outlet connected to a third conduit 104 upstream of the second channel 123, and a liquid outlet connected to the tank 200 via a pipe 143.

[0072] For example, due to pipe 143, the liquid phase of the gas contained in phase separator 134 can return to the bottom of tank 202, and the flow of this liquid gas depends on valve 135 installed on pipe 143.

[0073] According to the invention, the heat exchanger 121 is cooled by the gas flow in the first channel 122 and the second channel 123, particularly kept at a low temperature, but without condensation of the gas. When such condensation is required, this cooling of the heat exchanger 121 allows the gas to reach condensation conditions more quickly.

[0074] As described above, the cooling device 130 includes at least a control element 131. A “control element” refers to any component capable of changing the gas flow rate within the conduit through which the gas is delivered. In this case, the control element 131 may be a valve adapted to take at least one open position, at least one closed position, and multiple intermediate positions, whereby the control element allows gas flow in the open position, blocks gas flow in the closed position, and the intermediate positions allow control of the gas flow rate in the first channel 122.

[0075] like Figures 1 to 7 As shown, the control element 131 can be mounted on the fifth conduit 106, located upstream of the two-phase inlet of the phase separator 133. Alternatively or supplementarily, the control element 131 can be arranged on the sixth conduit 107, which extends between the gas outlet of the phase separator 133 and the third conduit 104. In any case, the control element 131 is arranged on a conduit that directly affects the flow rate of the gas flowing through the first channel 122 of the heat exchanger 121, particularly upstream or downstream of the heat exchanger 121.

[0076] The supply system 100 according to the invention is configured to implement the step of cooling the heat exchanger 121 of the condensing unit 120. For example, this cooling step is controlled by a cooling device 130. As detailed below, this method is capable of simultaneously supplying gas to the gas consuming device 101 and the heat exchanger 121 at a reduced gas flow rate, but still sufficient to cool or maintain the heat exchanger 121 at a temperature that allows the condensing unit 120 to operate in a reduced time.

[0077] The cooling process of the heat exchanger 121 is performed sequentially before the condensation process because it is designed to thermally prepare the heat exchanger for liquefaction and is carried out simultaneously with the supply process; therefore, the cooling is transparent from an energy perspective.

[0078] The cooling device 130 according to the invention is configured to take a portion of the gas supplied to the gas-consuming device 101 to cool the heat exchanger 121 of the condensing unit 120 or to keep it at a low temperature. In other words, the control member 131 is configured to take one of the aforementioned intermediate positions, which allows a flow rate between 50 kg / h and 300 kg / h to be obtained within the fifth conduit 106. Advantageously, the control member 131 is configured to take an intermediate position, due to which the gas flowing in the fourth conduit 105 has a flow rate equal to or substantially equal to 200 kg / h.

[0079] To avoid any thermal shock within the heat exchanger 121, the cooling device 130 includes a device 142 for controlling the temperature of the heat exchanger 121. As shown, the device 142 for controlling the temperature of the heat exchanger 121 includes at least one bypass conduit 140 for bypassing the second channel 123 of the heat exchanger 121.

[0080] As shown, the bypass conduit 140 extends between the tank top space 201 and the supply unit 110, allowing it to bypass the second passage 123 of the heat exchanger 121. More specifically, the bypass conduit 140 is configured such that gas following the bypass conduit 140 enters the pressure-increasing section 112. At least one flow regulating device 141 is arranged at the intersection between the third conduit 104 and the bypass conduit 140. According to the example shown, the flow regulating device 141 is a three-way valve adapted to take at least one first open position, at least one second open position, and a plurality of intermediate positions. In the first open position, the flow regulating device allows gas to flow only in the bypass conduit 140; in the second open position, the flow regulating device allows gas to flow only in the direction of the second passage 123 of the heat exchanger 121; and in the plurality of intermediate positions, the flow regulating device allows gas to flow at different flow rates in the bypass conduit 140 and in the direction of the second passage 123 of the heat exchanger 121, these flow rates being lower than the flow rate of gas when the flow regulating device 141 is in one of its open positions.

[0081] During the cooling step, the flow regulating device 141 is in an intermediate position, in which it allows gas to flow in the bypass duct 140, thereby causing the gas flow rate in the second channel 123 of the heat exchanger 121 of the condensing unit 120 to be between 37.5 kg / h and 405 kg / h. Advantageously, this flow rate is equal to or substantially equal to 230 kg / h. Generally, the flow regulating device 141 controls the gas flow rate through the second channel 123 of the heat exchanger 121 to be between 75% and 135% of the gas flow rate through the first channel 122 of the heat exchanger 121, which is between 50 kg / h and 300 kg / h.

[0082] It should be noted that the gas leaving the second channel 123 of the heat exchanger 121 and the gas flowing into the bypass conduit 140 merge at the second connection point 402, from which the sixth conduit 107 extends. Therefore, the gas leaving the heat exchanger 121 and the gas leaving the bypass conduit 140 mix upstream of the supply unit 110, more specifically, upstream of the pressure rise portion 112 of the supply unit 110. As shown, the sixth conduit 107 extends between the second connection point 402 and a third connection point 403 located upstream of the pressure rise portion 112 of the supply unit 110, particularly between the temperature rise portion 111 and the pressure rise portion 112 of the supply unit 110.

[0083] In other words, the system 100 is configured such that the gas leaving the second channel 123 of the heat exchanger 121 and the gas flowing into the bypass duct 140 are both subjected to a pressure increase imposed by the pressure increase portion 112 of the supply unit 110.

[0084] The gas flow rate through the bypass duct 140 depends on the gas temperature determined or measured at the inlet 144 of the first channel 122 of the heat exchanger 121. Therefore, the position of the flow regulating device 141 is determined by the gas temperature measured at the inlet 144.

[0085] For example, the gas temperature at the inlet 144 of the first channel 122 can be measured or determined by sensor 138, and the sensor probe can directly or indirectly contact the gas flowing in the relevant pipeline.

[0086] Control line 137 indicates the dependence of flow regulation device 141 on the gas temperature measured by sensor 138 at inlet 144.

[0087] This sensor 138 and control circuit 137 can be used as part of a device 142 for controlling the temperature of the heat exchanger 121.

[0088] Furthermore, the gas flow rate through the bypass duct 140 also depends on the gas temperature determined or measured at the outlet 139 of the second channel 123 of the heat exchanger 121. Therefore, the position of the flow regulating device 141 is also controlled by the gas temperature measured at the outlet 139.

[0089] For example, the gas temperature at the outlet 139 of the second channel 123 is measured or determined by the aforementioned sensor 138, whose probe may be in direct or indirect contact with the gas flowing in the relevant conduit, for example. Of course, such temperature may also be determined or measured by another sensor different from sensor 138.

[0090] Here, control line 137 again represents the dependence of flow regulation device 141 on the gas temperature measured by sensor 138 at outlet 139.

[0091] refer to Figures 2 to 4 The first embodiment of the present invention will be described below. Figure 2 The system 100 at the time of shutdown is shown. Figure 3 The system 100, in which heat exchanger 121 is cooled, and particularly kept cold by means of the method according to the invention, is shown. Figure 4 The system 100 used during the condensation phase is shown.

[0092] refer to Figures 5 to 7 The second embodiment of the present invention is described. Figure 5 The system 100 at the time of shutdown is shown. Figure 6 A system 100 is shown in which the heat exchanger 121 is cooled, and in particular kept cold by means of the method according to the invention. Figure 7 The system 100 used during the condensation phase is shown.

[0093] As described below, the main difference between the first and second embodiments lies in the components constituting the supply unit 110, particularly the components constituting the temperature rise portion 111 of the supply unit 110. Therefore, the components common to both embodiments and described above will not be repeated in detail.

[0094] according to Figures 2 to 4 In the first embodiment shown, the temperature rise section 111 of the supply unit 110 includes at least one heat exchanger 113, at least one expansion device 116, and at least one compression device 117.

[0095] The heat exchanger 113 includes at least one first line 114 and at least one second line 115, the first line 114 being supplied with liquid gas extracted from the tank 200, the second line 115 being supplied with liquid gas extracted from the tank, and an expansion device 116 being arranged between the tank 200 and the first line 114 of the heat exchanger 113. A compression device 117 is configured to increase the pressure of the gas flowing in the first line 114 of the heat exchanger 113 to at least atmospheric pressure.

[0096] The first line 114 is connected to the first pump 300 located at the bottom of the tank 202 on one side and to the compression device 117 on the other side. The second line 115 is connected to the second pump 301 located at the bottom of the tank 202 on one side and to the tank 200 on the other side, more specifically, to the bottom of the tank 202 in which liquid gas is stored.

[0097] In other words, the first conduit 102 extends between the first pump 300 and the first line 114 of the heat exchanger 113 and carries the expansion device 116, the seventh conduit 108 extends between the second pump 301 and the second line 115 of the heat exchanger 113, and the eighth conduit 109 extends between the second line 115 and the bottom of the tank 202.

[0098] Alternatively, the first and second lines of the heat exchanger can be supplied by the same pump, with a branching point provided between the single pump and the first and second lines of the heat exchanger.

[0099] An expansion device 116 is arranged on the first conduit 102, through which gas extracted in liquid form from the bottom of tank 202 by the first pump 300 expands before reaching the first line 114 of heat exchanger 113. In other words, the gas extracted in liquid form from the tank by the first pump 300 enters the heat exchanger 113 at a pressure below atmospheric pressure. A second pump 301 is configured to send the gas extracted in liquid form from the bottom of tank 202 directly to the second line 115 of heat exchanger 113, i.e., the gas extracted in liquid form from tank 200 does not undergo any change in temperature or pressure other than that associated with the pumping itself before entering the second line 115 of heat exchanger 113. Therefore, heat exchanger 113 is configured to perform heat exchange between the liquid gas extracted from the tank that has undergone a pressure reduction and the liquid gas extracted from the tank that has not undergone a pressure change. Thus, the liquefied gas flowing in the first line 114 is evaporated, while the liquefied gas flowing in the second line 115 is subcooled before returning to the bottom of tank 202. In other words, according to a first embodiment of the invention, the temperature-raising portion 111 of the supply unit 110 is more specifically a portion for evaporating at least a portion of the gas extracted in liquid form from the bottom of the tank 202.

[0100] In the presence of a second heat exchanger 145, the device includes a bypass passage 148 extending between the seventh conduit 108 and the eighth conduit 109, which is arranged in parallel with the second line 115 of the heat exchanger 113. The flow of liquid gas extracted from the tank within the bypass passage 148 and / or within the second line 115 depends on a control member 149, which may here be in the form of a three-way valve installed at the intersection of the bypass passage 148 and the seventh conduit 108 or between the bypass passage and the eighth conduit 109.

[0101] During the condensation phase, the liquid gas extracted from tank 200 enters the second heat exchanger 145 and passes through the second channel 147 of the second heat exchanger. The particularly low temperature of this liquid gas (approximately -163°C here) is used to promote the condensation of the gas entering the first channel 146 of the second heat exchanger 145.

[0102] Liquid gas flows into the first line 114 of heat exchanger 113 at a pressure below atmospheric pressure. To ensure this flow, a compression device 117, arranged between heat exchanger 113 and pressure riser section 112 of supply unit 110, is configured to return the gas leaving heat exchanger 113 to approximately atmospheric pressure. For example, the compression device 117 is configured to compress the gas from 0.35 bar to 1 bar. The compressed gas can then be added to pressure riser section 112 of supply unit 110, raising its pressure to a level appropriate for the needs of gas consumption device 101. Compression device 117 is arranged between heat exchanger 113 and third connection point 403, at which sixth conduit 107 engages with supply unit 110.

[0103] like Figure 3 As shown, the gas in the supply unit 110 and the tank top space 201 described above is supplied to the gas consumption device 101. During this operation phase, the heat exchanger 121 is cooled or kept cold due to the aforementioned cooling device 130. In other words, the first channel 122 of the heat exchanger 121 is supplied with the gas extracted from the second conduit 103 at a flow rate between 50 kg / h and 300 kg / h, advantageously equal to 200 kg / h. The second channel 123 is supplied with the gas extracted in gaseous form from the tank top space 201 at a flow rate between 37.5 kg / h and 405 kg / h, advantageously 230 kg / h. The bypass conduit 140 is supplied with the remaining portion of the gas extracted in gaseous form from the tank top space 201.

[0104] Therefore, the heat exchanger 121 can be put into use as soon as needed, for example, when the system 100 is in a situation where the amount of gaseous gas in the tank top space 201 is greater than the amount of gas consumed by the gas consuming device 101. This situation occurs, for example, in... Figure 4 As shown in the image.

[0105] When the amount of available gas in the top space 201 of the tank exceeds the amount of gas consumed by the gas consuming device 101, the condensing unit 120 liquefies the excess gas and returns it to the tank 200, thereby avoiding the loss of gas compressed by the compression section 112. In this condensing mode, the control component 131 is in the intermediate or open position to supply excess gas, i.e., gas that is in a gaseous state and compressed but not consumed by the gas consuming device 101, to the first channel 122 of the heat exchanger 121.

[0106] In this condensation step, gas that is not consumed by the gas consuming device 101 and has a flow rate higher than 300 kg / h is liquefied within the heat exchanger 121 so that it can be returned to the tank 200 in liquid form. During this condensation step, the gas flow rate within the first channel 122 of the heat exchanger 121 is higher than 300 kg / h and lower than 3000 kg / h.

[0107] Heat exchanger 121 is the site where heat exchange occurs between the gas flowing in the first channel 122 and the gas flowing in the second channel 123, so as to cool the gas flowing in the first channel 122 on the one hand and heat the gas flowing in the second channel 123 on the other. As a result, the gas flowing in the first channel 122 can then return to the second heat exchanger 145, where the gas is condensed by heat exchange between the gas flowing in the second channel 147 of the second heat exchanger 145 and the liquid gas extracted from the tank 200 by means of the seventh conduit 108 and the bypass channel 148. Afterwards, the gas flowing through the second channel 147 of the second heat exchanger 145 is added to the tank 200 via the eighth conduit 109.

[0108] Specifically, Figure 4 The diagram shows the flow regulating device 141 in the second open position, so there is no gas flow in the bypass conduit 140.

[0109] according to Figure 4 In the example shown, pumps 300 and 301, as well as the compressor 117, are stopped. In other words, the temperature rise section 111 of the supply unit 110 stops. In fact, the amount of gas naturally present in the tank top space 201 is sufficient to supply the gas consumption device 101, eliminating the need for evaporating liquefied gas for this supply. The cessation of this temperature rise section 111 allows for a reduction in the operating costs of the system 100 according to the invention.

[0110] Figures 5 to 7 The supply system 100 of the second embodiment shown differs from the system 100 of the first embodiment, particularly in the components constituting the temperature rise portion 111' of the supply unit 110. Furthermore, the second embodiment shown differs from the first embodiment shown in that the system 100 includes a refrigerant fluid circuit thermally associated with the supply unit 110.

[0111] According to the second embodiment, the refrigerant fluid circuit 500 includes at least one first heat exchanger 113', a compression device 501 adapted to increase the pressure of the refrigerant fluid flowing therethrough, at least one second heat exchanger 125, and at least one expansion device 502 adapted to decrease the pressure of the refrigerant fluid. The pressure-increasing section 111' includes at least the first heat exchanger 113'. The first heat exchanger 113' of the temperature-increasing section 111' includes at least one first line 114' supplied by gas extracted in a gaseous state from the tank top space 201 and at least one second line 115' supplied by gaseous refrigerant fluid and compressed by the compression device 501. Therefore, unlike the first embodiment, the first conduit 102' extends between the tank top space 201 and the first line 114' of the heat exchanger 113'.

[0112] The refrigerant fluid is selected such that the heat exchange occurring within the heat exchanger 113' results in an increase in the temperature of the gas flowing within the first line 114' of the heat exchanger 113'.

[0113] The second heat exchanger 125 further includes at least one first channel 126 and at least one second channel 127. The first channel 126 is supplied with liquid gas extracted from the bottom of the tank 202, and the second channel 127 is supplied with expanding refrigerant fluid. That is, the second heat exchanger 125 is directly disposed downstream of the expansion device 502 on the refrigerant fluid circuit 500. Therefore, the first channel 126 of the second heat exchanger 125 is supplied by a pump 303 arranged in the bottom of the tank 202.

[0114] Furthermore, the second channel 147 of the second heat exchanger 145 is connected to the first channel 126 of the second heat exchanger 125. In this way, the liquid gas that has been cooled by the second heat exchanger 125 promotes the condensation of the gas flowing through the first channel 122 of the first heat exchanger 121.

[0115] The refrigerant fluid flowing in the refrigerant fluid circuit 500 is circulated through a compression device 501, where its pressure increases. Therefore, it exits the compression device 501 in a gaseous and high-pressure state, and then enters a first heat exchanger 113', where it transfers heat to the gas flowing in the first line 114' of the heat exchanger 113'. Thus, the refrigerant fluid exits the second line 115' of the heat exchanger 113' in a two-phase or liquid state and enters an expansion device 502, where its pressure decreases. The refrigerant fluid then enters a second heat exchanger 125, where it absorbs heat from the gas extracted in a liquid state from the bottom of the tank 202. The heat exchange performed in the second heat exchanger 125 results in the evaporation of the refrigerant fluid, which can then initiate a new thermodynamic cycle and simultaneously subcool the gas extracted in a liquid state from the bottom of the tank 202. The subcooled gas is used in the second heat exchanger 145 to liquefy the gas from the first channel 122 of the first heat exchanger 121 before being sent back to the tank 200.

[0116] According to the example shown here, the first heat exchanger 113' advantageously includes a third channel 119' for supplying refrigerant fluid. Specifically, this third channel 119' is located in the refrigerant circuit 500 between the second channel 127 of the second heat exchanger 125 and the compression device 501. Thus, the second channel 115' and the third channel 119 form an internal heat exchanger of the refrigerant fluid circuit 500, which allows the gaseous gas leaving the second heat exchanger 125 to be preheated before entering the compression device 501, and the gaseous gas leaving the compression device 501 to be precooled before entering the expansion device 502. In other words, it should be understood that the presence of the third channel 119' in the first heat exchanger 113' improves the overall thermal performance of the refrigerant fluid circuit 500.

[0117] It should also be noted that, compared with the first embodiment, the temperature rise portion 111' according to the second embodiment does not include a compression device.

[0118] Finally, the supply system 100 according to the second embodiment differs from the supply system 100 according to the first embodiment in that it includes a forced evaporation line 128 extending from a pump 302 disposed at the bottom of the tank 202 to a third connection point 403 located upstream of the pressure rise section 112. Figure 6As schematically shown, a vaporizer 129 is arranged on the forced evaporation line 128. The evaporator 129 is configured to evaporate the gas extracted in liquid form by a pump 302 located at the bottom of tank 202. As detailed below, the forced evaporation line 128 is particularly useful when the gaseous gas present in the space at the top of the tank is insufficient to meet the needs of the gas consumption device 101.

[0119] According to a variation of the second embodiment not described herein, pump 302 can be a high-pressure pump, i.e., a pump configured to increase the pressure of the liquid it draws in. In this case, the high-pressure pump can, for example, be configured to increase the pressure of the extracted gas to between 1 bar and 400 bar, advantageously between 1 bar and 17 bar, and more advantageously between 6 bar and 17 bar. According to this alternative, evaporation line 128 then extends between the high-pressure pump and the second conduit 103, i.e., at a point downstream of the pressure-increasing portion of the supply unit.

[0120] Figure 6 and Figure 7 A supply system 100 is shown that is implemented during the step of cooling the heat exchanger and the step of using the condensing unit to at least partially liquefy the gas, according to a second embodiment of the present invention.

[0121] exist Figure 6 In the case shown, the amount of gas in the top space 201 of the tank is insufficient to supply the gas consumption device 101, so the forced evaporation line 128 is activated or the supply unit 110 is activated. Figure 6 Only the activation of the forced evaporation line 128 is shown. Therefore, before the pressure rise section of the supply unit 110 is added to finally supply the gas consumption device 101, the gas is extracted in liquid form from the bottom of the tank 202 and evaporated by the evaporator 129.

[0122] Similar to the manner described above with reference to the first embodiment, a portion of the gas flowing in the second conduit 103 is obtained by the cooling device 130 and supplied to the first channel 122 of the heat exchanger 121 at a flow rate of 50 kg / h to 300 kg / h (advantageously equal to 200 kg / h), so that the heat exchanger 121 can be operated quickly when the condensation step is performed. Similarly, a bypass conduit 140 of the second channel 123 of the heat exchanger 121 is supplied such that the gas flowing in the second channel 123 of the heat exchanger 121 has a flow rate including between 37.5 kg / h and 405 kg / h, advantageously equal to 230 kg / h.

[0123] Similar to the above, Figure 6 The implementation of the system during the cooling steps shown Figure 3 The implementation of system 100 shown is the same or nearly the same.

[0124] exist Figure 7In the illustrated case, the forced evaporation line 128 is stopped, and only the gaseous gas extracted from the tank top space 201 is supplied to the gas consuming device 101. In this case, the condensation unit 120 condenses the gas that was not consumed by the gas consuming device 101. For this purpose, the flow regulating device 141 is in its second open position, that is, all the gas extracted by the third conduit 104 is sent to the second channel 123 of the heat exchanger 121.

[0125] at last, Figure 8 This is a cross-sectional view of vessel 70, which includes tanks 200 containing liquid and gaseous gases. Tanks 200 are prismatic in shape and are mounted on the vessel's double hull 72. Tank 200 can be part of an LNG carrier, but it can also be an oil tank when the gas is used as fuel for fuel-consuming equipment.

[0126] The wall of tank 200 has a primary sealing membrane for contact with the liquid gas in the tank, a secondary sealing membrane disposed between the primary sealing membrane and the double hull 72 of the vessel 70, and two thermal barriers disposed between the primary sealing membrane and the secondary sealing membrane and between the secondary sealing membrane and the double hull 72, respectively.

[0127] Loading and / or unloading pipelines 73, located on the upper deck of the ship, can be connected to a seaport or port terminal via suitable connectors to transport liquefied natural gas cargo from or to tank 200.

[0128] Figure 8 An example of a maritime terminal with a loading and / or unloading station 75, an underwater conduit 76, a shore or port facility 77, and conduits 74, 78 is also shown. The loading and unloading station 75 enables the vessel 70 to be loaded and / or unloaded from or to the shore facility 77. The latter includes a liquefied gas storage tank 80 and a connecting conduit 81 that connects to the loading and / or unloading pipeline 73 via the underwater conduit 76. The underwater conduit 76 enables the transport of liquefied gas over long distances, such as 5 kilometers, between the loading or unloading station 75 and the shore facility 77, allowing the vessel 70 to remain away from the coast during loading and / or unloading operations.

[0129] To generate the pressure required for transporting liquefied gas, one or more unloading pumps carried by the loading and / or unloading tower of tank 200 and / or pumps equipped on land facility 77 and / or pumps equipped at loading and unloading station 75 are implemented.

[0130] Therefore, the present invention provides a gas supply system that can supply naturally evaporated gas and forced-evaporation liquefied gas to gas-consuming equipment on board. If the energy demand of the naturally evaporated gas is too high relative to the energy demand of the ship's (ducted) gas-consuming equipment, the naturally evaporated gas can also be condensed. Before this condensation step, there is a step of cooling the heat exchanger of the condensation unit. Therefore, compared with the prior art, the condensation unit can operate in a shorter time.

[0131] However, the invention is not limited to the devices and configurations described and shown herein, but extends to any equivalent devices or configurations and any combination of technologies using such devices.

Claims

1. A method for supplying gas to a gas-consuming device (101), the gas-consuming device being disposed on a ship, the ship including a tank (200) containing liquid and gaseous gases, the method comprising at least: The step of supplying gas extracted in gaseous form from the tank (200) to the gas consuming device (101) via the supply unit (110) A condensation step is performed by means of a condensation unit (120) comprising at least one heat exchanger (121) for condensing at least a portion of the gas extracted in gaseous form from the tank (200), the heat exchanger comprising at least one first channel (122) and a second channel (123), the heat exchanger (121) being configured to exchange heat between the extracted gas flowing in the first channel (122) between the supply unit (110) and the gas consumption device (101) and between the gas flowing in the second channel (123) between the tank (200) and the supply unit (110), the supply method being characterized in that it comprises a cooling step for cooling the heat exchanger (121) by means of an airflow in the first channel (122) and an airflow in the second channel (123) of the heat exchanger (121), the cooling step being performed prior to the condensation step and at least partially concurrent with the supply step.

2. The supply method according to claim 1, wherein, The cooling step includes controlling the flow rate of gas flowing through the first channel (122) of the heat exchanger (121) to a ratio between 2% and 12% of the flow rate of gas extracted in gaseous form from the tank (200) during the supply step.

3. The supply method according to claim 1 or 2, wherein, The cooling step includes controlling the gas flow rate through the second channel (123) of the heat exchanger (121) during the cooling step to a ratio between 75% and 135% of the gas flow rate through the first channel (122) of the heat exchanger (121).

4. The supply method according to claim 1 or 2, wherein, The cooling step includes controlling the gas flow rate through the first channel (122) of the heat exchanger (121) during the cooling step to a value between 50 kg / h and 300 kg / h.

5. The supply method according to claim 1 or 2, wherein, The gas flow rate through the first channel (122) of the heat exchanger (121) during the cooling step includes between 3% and 20% of the gas flow rate through the first channel (122) of the heat exchanger (121) during the condensation step.

6. The supply method according to claim 2, wherein, During the cooling step, gas flowing through the first channel (122) of the heat exchanger (121) is added to the supply unit (110).

7. The supply method according to claim 1 or 2, wherein, The cooling step of cooling the heat exchanger (121) is the step of cooling the heat exchanger (121) to cause the heat exchanger (121) to change from a positive temperature to a negative temperature.

8. The supply method according to claim 1 or 2, wherein, The cooling step of cooling the heat exchanger (121) is a step of keeping the heat exchanger (121) cold so that the heat exchanger (121) changes from a first negative temperature to a second negative temperature.

9. A gas supply system (100) for performing the supply method according to claim 1, said gas supply system (100) comprising at least: Tanks (200) for storing and / or transporting liquid and gaseous gases, for containing gases, The supply unit (110) for the gas consuming device (101) is configured to extract gas from the tank (200) and increase the gas pressure to supply the gas consuming device (101). The condensing unit (120) includes at least one heat exchanger (121) having a first channel (122) and a second channel (123). The condensing unit (120) is configured such that extracted gas between the supply unit (110) and the gas consumption device (101) flows through the first channel (122), while gas flowing between the tank (200) and the supply unit (110) flows through the second channel (123). The apparatus (130) for cooling the heat exchanger (121) includes: at least one control member (131) configured to control the flow rate of gas flowing through the first channel (122); and means (142) for controlling the temperature of the heat exchanger (121) cooled by airflow in the first channel (122) and the second channel (123).

10. The gas supply system (100) according to claim 9, wherein, The device (142) for controlling the temperature of the heat exchanger (121) includes at least one bypass conduit (140) for bypassing a second channel (123) of the heat exchanger (121).

11. The gas supply system (100) according to claim 10, wherein, The device (142) for controlling the temperature of the heat exchanger (121) includes at least one device (141) for regulating the flow rate of gas flowing through the bypass duct (140) and a sensor (138) capable of measuring or determining the gas temperature at the inlet (144) of the first channel (122) of the heat exchanger (121), the flow rate of gas flowing through the bypass duct (140) depending at least on the gas temperature determined at the inlet (144) of the first channel (122) of the heat exchanger (121).

12. The gas supply system (100) according to claim 11, wherein, The sensor (138) is capable of measuring or determining the gas temperature at the outlet (139) of the second channel (123) of the heat exchanger (121), and the flow rate of the gas flowing through the bypass duct (140) depends on the gas temperature at the outlet (139) of the second channel (123) of the heat exchanger (121).

13. The gas supply system (100) according to any one of claims 9 to 12, wherein, The condensing unit (120) includes at least a first heat exchanger (121), which includes a first channel (122) and a second channel (123). The condensing unit (120) also includes a second heat exchanger (145), which is a heat exchange site between gas extracted in liquid form from the tank (200) and gas from the first channel (122) of the first heat exchanger (121).

14. The gas supply system (100) according to any one of claims 9 to 12, wherein, The supply unit (110) includes at least one temperature raising section (111) for raising the temperature of the gas extracted in liquid form from the tank (200) and at least one pressure raising section (112) for raising the gas pressure to supply the gas consumption device (101).

15. The gas supply system (100) according to claim 14, wherein, The temperature rise section (111) of the supply unit (110) includes at least one heat exchanger (113) and at least one compression device (117), the compression device (117) being arranged between the heat exchanger (113) and the pressure rise section (112), the heat exchanger (113) including at least one first line (114) and at least one second line (115), the first line (114) being supplied with gas extracted in liquid form from the tank (200), the second line (115) being supplied with gas extracted in liquid form from the tank (200), and at least one expansion device (116) being arranged between the tank (200) and the first line (114) of the heat exchanger (113).

16. A ship (70) for transporting liquid gas, comprising at least one gas supply system (100) according to any one of claims 9 to 15.

17. A system (100) for loading or unloading liquid gas, comprising at least one onshore or port facility (77) and at least one vessel (70) for transporting liquid gas according to claim 16.

18. A method for loading or unloading liquid gas for a ship (70) for transporting gas according to claim 16, wherein during the method, the liquid gas is transported via pipes (76, 78, 79, 81) from a tank (200) of the ship (70) toward a floating or onshore storage facility (77) or from a floating or onshore storage facility (77) toward a tank (200) of the ship (70).

Images