Installation comprising a floating platform intended for intermittently receiving a co2 rich feed from off-loading ships, and for delivering a co2 rich flow intended to be injected underground

Abstract

An installation comprising a platform (12) floating on a body of water (48) for intermittently receiving a CO2 rich feed (14) from off-loading ships (16), and for delivering a CO2 rich flow (18) intended to be injected underground, comprising: - a storage unit (50) for storing the feed (14) and for delivering a liquid flow (56), - a compression unit (60), - a liquefaction unit (66) with heat exchange with a part of the liquid flow (56), - a separation unit (72) for obtaining a liquid flow (74) received in the storage unit, - a vaporizing unit (78) adapted for vaporizing a liquid flow (80) including at least a part of the first liquid flow to obtain a gas flow (84) received in the storage unit, - a thermal unit (86) adapted for providing the heating fluid, and for performing a heat exchange with water (88). The platform is configured for switching at least between two operation modes.

Description

FIELD

[0001] The present disclosure deals with an installation comprising a platform for delivering a CO2 rich flow intended to be injected underground.

[0002] The disclosure also deals with a process using such an installation, comprising delivering the CO2 rich flow.BACKGROUND

[0003] Usually CO2 capture and sequestration is performed onshore because CO2 sources are onshore and for convenience.

[0004] However, it would be desirable to use some offshore sites for doing so, in particular where a traditional oil and gas offshore platform already exists and could perform the injection.

[0005] One issue is then how to transport CO2 to the existing offshore platform. Installing a CO2 pipeline would not be practical, as the injection sites are typically a few hundreds of kilometers offshore.

[0006] One solution could consist in using an additional floating platform located next to the existing platform and feeding the latter from CO2 carrying ships coming from one or several harbors. The floating platform could receive an intermittent CO2 feed from the CO2 carrying ships and deliver a continuous CO2 flow to the existing platform, which could perform the injection without having to be much modified.

[0007] However, off-loading large amounts of CO2 from a ship to a platform via one or several lines generates a lot of CO2 vapor which cannot be returned to the off-loading ship and thus has to be vented to the atmosphere.

[0008] An objective of the disclosure is to solve or reduce the above issues by providing an installation able to deliver a CO2 rich flow intended to be injected offshore, with limited CO2 venting and in a cost efficient manner.SUMMARY OF THE INVENTION

[0009] To this end, the disclosure proposes an installation comprising a floating platform intended for intermittently receiving a CO2 rich feed from off-loading ships, and for delivering a CO2 rich flow intended to be injected underground, the platform comprising a platform adapted for floating on a body of water and intended for intermittently receiving a CO2 rich feed from off-loading ships, and for delivering a CO2 rich flow intended to be injected underground, the platform comprising: a storage unit adapted for receiving the feed, for storing the feed as one or several liquid phase(s) and one or several vapor phase(s), and for delivering a first liquid flow from the liquid phase(s), the delivered flow being obtained using a second liquid flow including at least a part of the first liquid flow, a compression unit adapted for receiving a first gas flow from the storage unit and for compressing the first gas flow in order to obtain a pressurized gas flow, a liquefaction unit adapted for at least partly liquefying the pressurized gas flow by a first heat exchange with a first cooling fluid in order to obtain an at least partly liquefied flow, the first cooling fluid being a part of the first liquid flow, a separation unit adapted for separating the at least partly liquefied flow into a third liquid flow and a second gas flow, the storage unit being adapted for receiving the third liquid flow, a vaporizing unit adapted for vaporizing a fourth liquid flow by a second heat exchange with a first heating fluid in order to obtain a third gas flow, the fourth liquid flow including at least a part of the first liquid flow, and the storage unit being adapted for receiving the third gas flow, and a thermal unit adapted for providing the first heating fluid, and for performing a third heat exchange with water coming from the body of water, wherein the platform is configured for switching at least between: a first operation mode, in which: the storage unit receives the feed and produces the first gas flow from the vapor phase(s) ; the third liquid flow is produced and received in the storage unit; and the third gas flow is not produced, and a second operation mode, in which: the storage unit does not receive the feed ; the third gas flow is produced and received in the storage unit in order to form a part of the vapor phase(s) ; and the third liquid flow is not produced.

[0010] In other embodiments, the installation may comprise one or several of the following features, taken in isolation or any technically feasible combination: the platform comprises a conditioning unit adapted for heating the second liquid flow by a fourth heat exchange with a second heating fluid, and for increasing a pressure of the second liquid flow in order to obtain the delivered flow, the thermal unit being adapted for providing the second heating fluid; the liquefaction unit is adapted for precooling the pressurized gas flow by a fifth heat exchange with a second cooling fluid prior to the first heat exchange with the first cooling fluid, the thermal unit being adapted for providing the second cooling fluid; the pressurized gas flow is at a temperature comprised between 50°C and 90°C before the fifth heat exchange, and at a temperature comprised between 0°C and 20°C after the fifth heat exchange and before the second heat exchange; the separation unit comprises a venting system adapted for venting at least part of the second gas flow; the platform comprises: a purification unit adapted for receiving the second gas flow and a fifth liquid flow, and for producing a fourth gas flow and a sixth liquid flow, the fifth liquid flow comprising a part of the first liquid flow, the second liquid flow comprising the sixth liquid flow, a mass flow of CO2 being smaller in the fourth gas flow than in the second gas flow; and a venting system adapted for venting the fourth gas flow; the purification unit comprises a purification column, at least part of the fourth gas flow being collected at the top of the purification column, at least part of the sixth liquid flow being collected at the bottom of the purification column; the first heating fluid comprises glycolated water; the thermal unit is adapted for recovering the first heating fluid after the second heat exchange from the vaporizing unit in the second operating mode in order to obtain a recovered flow, and for heating at least a part of the recovered flow by the third heat exchange in order to obtain a heated flow, the first heating fluid comprising at least a part of the heated flow; the thermal unit is adapted for splitting the recovered flow at least into the part intended to be heated by the third heat exchange, and into a second cooling fluid, the liquefaction unit being adapted for precooling the pressurized gas flow by heat exchange with the second cooling fluid; the thermal unit forms a loop comprising a pumping system, a make-up tank, and a heat exchanger adapted for performing the third heat exchange; the separation unit comprises a drum, and / or the compression unit comprises a scrubber adapted for scrubbing the first gas flow, and at least one compressor adapted for pressurizing the first gas flow after said scrubbing; the storage unit is designed for receiving the feed at a pressure comprised between 7 and 45 bar absolute, and for delivering the first liquid flow (56) at a pressure comprised between 20 and 70 bar absolute; and / or the compression unit is designed for obtaining the pressurized gas flow at a pressure comprised between 40 and 80 bar absolute; and the installation comprises a second platform adapted for injecting the delivered flow underground, for producing power, and for delivering a part of said power to the floating platform.

[0011] The disclosure also proposes a process comprising: obtaining an installation as described above, intermittently receiving the CO2 rich feed from off-loading ships, delivering the CO2 rich flow, receiving and storing the feed in the storage unit, and delivering the first liquid flow from the liquid phase(s), obtaining the delivered flow using a second liquid flow including at least a part of the first liquid flow, receiving the first gas flow in the compression unit from the storage unit and compressing the first gas flow in order to obtain the pressurized gas flow, at least partly liquefying the pressurized gas flow in the liquefaction unit by the first heat exchange with the first cooling fluid in order to obtain the at least partly liquefied flow, separating the at least partly liquefied flow in the separation unit into the third liquid flow and the second gas flow, and receiving the third liquid flow in the storage unit, vaporizing the fourth liquid flow in the vaporizing unit by the second heat exchange with the first heating fluid in order to obtain the third gas flow, and receiving the third gas flow in the storage unit, obtaining the first heating fluid from the thermal unit, and performing the third heat exchange in the thermal unit with water coming from the body of water, and switching the platform at least between the first operation mode and the second operation mode. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] The disclosure and its advantages will be better understood upon reading the following description, given solely by way of example and with reference to the appended drawings, in which: Figure 1 is a schematic perspective view of an installation according to the disclosure, Figure 2 is a main process flow diagram of a floating platform shown in Figure 1, and Figure 3 is a process flow diagram of a thermal unit of the floating platform shown in Figure 1. DETAILED DESCRIPTIONInstallation

[0013] With reference to Figure 1, an installation 10 according to the invention will be described.

[0014] The installation 10 comprises a floating platform 12 intended for intermittently receiving a CO2 rich feed 14 from off-loading ships 16, 17 (of which two are represented in Figure 1), and for delivering a CO2 rich flow 18 intended to be injected underground.

[0015] In the example, the installation 10 comprises a second platform 20 adapted for injecting the delivered flow 18 underground (stream 22), for producing power, and for delivering a part 24 of said power to the floating platform 12.

[0016] The installation 10 advantageously comprises a control platform 26 located away from the second platform.

[0017] As a variant (not shown), the installation 10 does not comprise the second platform 20, the delivered flow 18 being injected by another piece of equipment (not shown).Off-loading ships

[0018] The off-loading ships 16, 17 are advantageously adapted for carrying 10000 to 20000 m 3< of liquid CO2, for example 12000 m 3< .

[0019] The off-loading ships 16, 17 for example come from a harbor 28 where they are filled with CO2. In Figure 1, the ship 17 is being filled with CO2, while the ship 16 is off-loading CO2.

[0020] A bow-stern off-loading system 30 is for example used to carry the CO2 rich feed 14 from the off-loading ship 16 towards the platform 12. The off-loading system 30 does not allow CO2 vapor to be returned to the ship 16.

[0021] The CO2 rich feed 14 for example comprises more than 90 mol.% of CO2, preferably more than 95 mol.% CO2, and more preferably more than 99.0 mol.% of CO2. The feed 14 may comprise other compounds, such as N2, CH4, CO, H2S, H2, water, O2, Ar and SO2.Second platform and control platform

[0022] The second platform 20 and the control platform 26 are for example supported by a sea bottom 32.

[0023] The second platform 20 is for example adapted for extracting a raw stream 34 comprising hydrocarbon compounds and for exporting a gas stream 36 and a liquid stream 38.

[0024] The second platform 20 is advantageously adapted for receiving another CO2 rich stream 40 intended to be injected underground.

[0025] The second platform 20 is connected to the floating platform by a transfer flexible line 42 for receiving the delivered flow 18, and by another line 44 for sending said power 24 and advantageously controlling the floating platform 12. The second platform 20 is for example 1.0 to 5.0 km away from the floating platform 12.

[0026] The lines 42, 44 are for example between 2.0 and 4.5 km long.

[0027] The second platform 20 is connected to the control platform 26 by a line 46 for being controlled.Floating platform

[0028] The platform 12 floats on a body of water 48, such as an ocean, a sea or a lake. In the example, the platform 12 is a few hundreds of kilometers away from the harbor 28, for example 500 km away. As a variant, the platform 12 is closer to the harbor 28.

[0029] As shown in Figure 2, the platform 12 comprises a storage unit 50 adapted for receiving the feed 14, for storing the feed as one or several liquid phase(s) 52 and one or several vapor phase(s) 54, and for exporting a first liquid flow 56 from the liquid phase(s). The delivered flow 18 is obtained using a second liquid flow 58 including at least a part of the first liquid flow 56.

[0030] The platform 12 comprises a compression unit 60 adapted for receiving and compressing a first gas flow 62 from the storage unit 50, in order to obtain a pressurized gas flow 64.

[0031] The platform 12 comprises a liquefaction unit 66 adapted for at least partly liquefying the pressurized gas flow 64 by a first heat exchange with a first cooling fluid 68 in order to obtain an at least partly liquefied flow 70, the first cooling fluid being a part of the first liquid flow 56.

[0032] The platform 12 comprises a separation unit 72 adapted for separating the at least partly liquefied flow 70 into a third liquid flow 74 and a second gas flow 76, the storage unit 50 being adapted for receiving the third liquid flow.

[0033] The platform 12 comprises a vaporizing unit 78 adapted for vaporizing a fourth liquid flow 80 by a second heat exchange with a first heating fluid 82 in order to obtain a third gas flow 84, the fourth liquid flow 80 including at least a part of the first liquid flow 56, and the storage unit 50 being adapted for receiving the third gas flow.

[0034] The platform 12 comprises a thermal unit 86 (figure 3) adapted for providing the first heating fluid 82, and for performing a third heat exchange with water 88 coming from the body of water 48.

[0035] In the example, the installation 10 comprises a conditioning unit 90 adapted for heating the second liquid flow 58 by a fourth heat exchange with a second heating fluid 92, and for increasing the pressure of the second liquid flow in order to obtain the delivered flow 18.

[0036] As a less preferred variant (not shown), the platform 12 does not comprise a conditioning unit, and the second platform 20 is for example adapted for heating the delivered flow 18 and increasing its pressure before injecting underground. In other words, the conditioning unit 90 is not in the platform 12 but in the second platform 20.

[0037] In the example, the platform 12 comprises a purification unit 94 adapted for receiving the second gas flow 76 and a fifth liquid flow 96, and for producing a fourth gas flow 98 and a sixth liquid flow 99, the fifth liquid flow 96 being a part of the first liquid flow 56, the second liquid flow 58 comprising the sixth liquid flow 99. The mass flow of CO2 is smaller in the fourth gas flow 98 than in the second gas flow 76.

[0038] In the example, the platform 12 comprises a venting system 100 adapted for venting the fourth gas flow 98.

[0039] As a less preferred variant (not shown), the platform 12 does not comprise the purification unit 94, and comprises a venting system (not shown) adapted for venting at least part of the second gas flow 76.

[0040] In a particular embodiment, the platform 10 comprises the two venting systems.

[0041] The platform 12 is configured for switching at least between a first operation mode and a second operation mode.

[0042] In the first operation mode, or "receiving" mode, the storage unit 50 receives the feed 14 and produces the first gas flow 62 from an excess in the vapor phase(s) 54, the third liquid flow 74 is produced and received in the storage unit 50, and the third gas flow 84 is not produced.

[0043] In the second operation mode, or "holding" mode, the storage unit 50 does not receive the feed 14, the third gas flow 84 is produced and received in the storage unit 50 in order to form a part of the vapor phase(s) 54, and the third liquid flow 74 is not produced.Storage unit

[0044] For example, the storage unit 50 comprises a plurality of storage tanks 102 (Figure 1), of which only one is represented in Figure 2.

[0045] The storage tanks 102 respectively for example contain several liquid phases 52, and several disconnected vapor phases 54.

[0046] As a variant, the storage tanks 102 are connected to each other, such that there is only one vapor phase 54.

[0047] According to another variant (not shown), the storage unit 50 comprises one storage tank 102.

[0048] For example, the storage unit 50 is designed for receiving the feed 14 at a pressure (internal pressure of the storage tank(s)) comprised between 7 and 45 bar absolute, preferably between 10 and 20 bar absolute, and for exporting the first liquid flow 56 at a pressure comprised between 20 and 70 bar absolute.

[0049] The first liquid flow 56 for example has a temperature comprised between -45°C and -10°C, preferably between -35°C and -25°C.

[0050] In a particular embodiment, the pressure in the storage tanks 102 is comprised between 14 and 18 bar absolute.

[0051] In other embodiments, the pressure in the storage tanks 102 is comprised between 7 and 10 bar absolute (low pressure storage) or between 35 and 45 bar absolute (high pressure storage).

[0052] The first gas flow 62 is obtained from an excess of the vapor phase(s) 54 in the storage unit 50.Compression unit

[0053] The compression unit 60 advantageously comprises a scrubber 104 adapted for scrubbing the first gas flow 62, and one or several compressor(s) 106 adapted for pressurizing the first gas flow 62 after said scrubbing.

[0054] Advantageously, the pressure of the pressurized gas flow 64 is comprised between 40 and 80 bar absolute, and is for example approximately 44 bar absolute.

[0055] The temperature of the pressurized gas flow 64 is for example comprised between 55°C and 90°C.Liquefaction unit

[0056] For example, the liquefaction unit 66 comprises two heat exchangers 108, 110.

[0057] The liquefaction unit 66 is advantageously adapted for precooling the pressurized gas flow 64 by a fifth heat exchange with a second cooling fluid 112, for example in the exchanger 108, prior to the first heat exchange with the first cooling fluid 68, which for example takes place in the heat exchanger 110.

[0058] For example, the pressurized gas flow 64 is at a temperature comprised between 50°C and 90°C before the fifth heat exchange (pre-cooling), and at a temperature comprised between 0°C and 20°C after the fifth heat exchange and before the second heat exchange.

[0059] The heat exchanger 110 is a CO2 / CO2 heat exchanger.

[0060] The temperature of the at least partly liquefied flow 70 is for example comprised between -30°C and -20°C.Separation unit and purification unit

[0061] The separation unit 72 for example comprises a drum 114.

[0062] For example, the purification unit 94 comprises a purification column 116, at least part of the fourth gas flow 98 being collected at the top of the purification column, at least part of the sixth liquid flow 99 being collected at the bottom of the purification column: The fourth gas flow 98 and the sixth liquid flow 99 for example have a temperature comprised between -33°C and -18°C.Vaporizing unit

[0063] The vaporizing unit 78 for example comprises a heat exchanger 118 adapted for performing the second heat exchange.Conditioning unit

[0064] Advantageously, the conditioning unit 90 comprises a heat exchanger 120 adapted for performing the fourth heat exchange, and a pump 122 or a pumping system (not shown) adapted for increasing the pressure of the second liquid flow 58 in order to obtain the delivered flow 18.

[0065] For example, the temperature of the second liquid flow 58 just after the fourth heat exchange is comprised between -2°C and 12°C.

[0066] The pressure of the delivered flow 18 is for example comprised between 45 and 150 bar absolute.

[0067] The pressure of delivered flow 18 may be increased by the second platform 20, for example above 300 bar absolute prior to injection.Thermal unit

[0068] The thermal unit 86 is advantageously adapted for providing the second cooling fluid 112 and the second heating fluid 92.

[0069] Advantageously, the thermal unit 86 is adapted for recovering the first heating fluid 82 after the second heat exchange from the vaporizing unit 78 in the second operating mode, and for heating at least a part 124 of the recovered flow 126 by the third heat exchange in order to obtain a heated flow 128, the first heating fluid 82 comprising at least a part of the heated flow 128.

[0070] Advantageously, the thermal unit 86 is also adapted for recovering the second heating fluid 92 after the fourth heat exchange from the conditioning unit 90 in order to obtain the recovered flow 126.

[0071] The thermal unit 86 is advantageously adapted for splitting the recovered flow 126 at least into the part 124 intended to be heated by the third heat exchange, and into the second cooling fluid 112 used in the liquefaction unit 66.

[0072] The thermal unit 86 for example forms a loop 128 comprising a pumping system 130, a make-up tank 132, and a heat exchanger 134 adapted for performing the third heat exchange.

[0073] The second cooling fluid 112, the first heating fluid 82 and the second heating fluid 92 for example comprise glycolated water, or are made of glycolated water.

[0074] The recovered flow 126 is for example at a temperature comprised between -9°C and -5°C.

[0075] The sea water 88 is for example at a temperature comprised between 4°C and 18°C before the third heat exchange, and at a temperature comprised between 0°C and 14°C after the third heat exchange.

[0076] The heated flow 128 is for example at a temperature comprised between 1°C and 15°C.

[0077] The first heating fluid 82 and the second heating fluid 92 are for example at a temperature comprised between 1°C and 15°C.Operation of the installation

[0078] The operation of the installation 10 stems for its above described structure and will now be described to illustrate a process according to the disclosure.

[0079] The CO2 rich feed 14 is intermittently received from the off-loading ships 16, 17, and the platform 12 delivers the CO2 rich flow 18, preferably on a continuous basis.

[0080] The first liquid flow 56 is exported by the storage unit 50 from the liquid phase(s) 52. The delivered flow 18 is obtained using the second liquid flow 58 which includes at least a part of the first liquid flow 56.

[0081] When an off-loading ship 16 is ready to deliver the feed 14, the platform 12 may be switched to the first operation mode, for example in case of an excess of vapor in the storage unit 50.

[0082] In the first operation mode, the storage unit 50 receives the feed 14 and produces the first gas flow 62 from the vapor phase(s) 54. The third liquid flow 74 is produced and received in the storage unit 50. The third gas flow 84 is not produced.

[0083] The first gas flow 62 is received in the compression unit 60 from the storage unit 50 and compressed in order to obtain the pressurized gas flow 64.

[0084] The pressurized gas flow 64 is at least partly liquefied in the liquefaction unit 66 by the first heat exchange with the first cooling fluid 68 in order to obtain the at least partly liquefied flow 70.

[0085] Advantageously, the pressurized gas flow 64 is precooled by the fifth heat exchange with the second cooling fluid 112.

[0086] The at least partly liquefied flow 70 is separated in the separation unit 72 into the third liquid flow 74 and the second gas flow 76.

[0087] In the example, the conditioning unit 90 heats the second liquid flow 58 by the fourth heat exchange with the second heating fluid 92, and increases the pressure of the second liquid flow 58 in order to obtain the delivered flow 18.

[0088] The thermal unit 86 performs the third heat exchange with water 88 coming from the body of water 48. In the example, the thermal unit 86 provides the second heating fluid 92 and the second cooling fluid 112.

[0089] In the example, the purification unit 94 receives the second gas flow 76 and the fifth liquid flow 96, and produces the fourth gas flow 98 and the sixth liquid flow 99. The fifth liquid flow 96 is a part of the first liquid flow 56, and the second liquid flow 58 comprises the sixth liquid flow 99. The fourth gas flow 98 is vented by the venting system 100.

[0090] When no off-loading ship delivers the feed 14, the platform 12 may be switched to the second operation mode, for example in case there is not enough vapor in the storage unit 50.

[0091] In the second operation mode, the storage unit 50 does not receive the feed 14. The third gas flow 84 is produced and received in the storage unit in order to form a part of the vapor phase(s) 54. The third liquid flow 74 is not produced (nor received in the storage unit).

[0092] The fourth liquid flow 80 is vaporized in the vaporizing unit 78 by the second heat exchange with the first heating fluid 82 in order to obtain the third gas flow 84. The first heating fluid 82 is provided by the thermal unit 86.Advantages

[0093] Thanks to the above described features, the installation 10 is able to deliver the CO2 rich flow 18 intended to be injected offshore, with limited CO2 venting and in a cost efficient manner. Indeed, when the feed 14 is received in the storage unit 50, little CO2 is vented thanks to the first operation mode, in which part of the vapor phase(s) 54 is converted into the third liquid flow 74 returned to the storage unit 50. When no feed 14 is received, part of the first liquid flow 56 is vaporized and fed into the vapor phases(s) 54 in the storage unit, thanks to the second operation mode.

[0094] Advantageously, the liquefaction unit 66 performs a CO2 / CO2 heat exchange, as the liquefaction unit uses a CO2 rich flow (a part of the first liquid flow 56) as a main cooling fluid.

[0095] The thermal unit 86 advantageously allows using heat coming from the body of water 48 without putting CO 2 flows in direct heat exchange with the water 88. Glycolated water is advantageously used as an intermediate thermal fluid.

[0096] Advantageously, the optional purification 94 unit allows further reducing the amount of vented CO2, as the mass flow of CO2 is smaller in the fourth gas flow 98 than in the second gas flow 76.

[0097] Advantageously, the liquefaction unit 66 allows significant energy savings by cooling the pressurized gas flow 64 that needs to be liquefied with the already available cold CO2 and at the same time heating the cold CO2 intended to be exported. This configuration avoids using additional cooling / heating utilities to fulfill this duty.

Claims

1. An installation (10) comprising a platform (12) adapted for floating on a body of water (48) and intended for intermittently receiving a CO2 rich feed (14) from off-loading ships (16, 17), and for delivering a CO2 rich flow (18) intended to be injected underground, the platform (12) comprising: - a storage unit (50) adapted for receiving the feed (14), for storing the feed (14) as one or several liquid phase(s) (52) and one or several vapor phase(s) (54), and for delivering a first liquid flow (56) from the liquid phase(s) (52), the delivered flow (18) being obtained using a second liquid flow (58) including at least a part of the first liquid flow (56), - a compression unit (60) adapted for receiving a first gas flow (62) from the storage unit (50) and for compressing the first gas flow (62) in order to obtain a pressurized gas flow (64), - a liquefaction unit (66) adapted for at least partly liquefying the pressurized gas flow (64) by a first heat exchange with a first cooling fluid (68) in order to obtain an at least partly liquefied flow (70), the first cooling fluid (68) being a part of the first liquid flow (56), - a separation unit (72) adapted for separating the at least partly liquefied flow (70) into a third liquid flow (74) and a second gas flow (76), the storage unit (50) being adapted for receiving the third liquid flow (74), - a vaporizing unit (78) adapted for vaporizing a fourth liquid flow (80) by a second heat exchange with a first heating fluid (82) in order to obtain a third gas flow (84), the fourth liquid flow (80) including at least a part of the first liquid flow (56), and the storage unit (50) being adapted for receiving the third gas flow (84), and - a thermal unit (86) adapted for providing the first heating fluid (82), and for performing a third heat exchange with water (88) coming from the body of water (48), wherein the platform (12) is configured for switching at least between: - a first operation mode, in which: the storage unit (50) receives the feed (14) and produces the first gas flow (62) from the vapor phase(s) (54); the third liquid flow (74) is produced and received in the storage unit (50); and the third gas flow (84) is not produced, and - a second operation mode, in which: the storage unit (50) does not receive the feed (14); the third gas flow (84) is produced and received in the storage unit (50) in order to form a part of the vapor phase(s) (54); and the third liquid flow (74) is not produced.

2. The installation (10) according to claim 1, wherein the platform (12) comprises a conditioning unit (90) adapted for heating the second liquid flow (58) by a fourth heat exchange with a second heating fluid (92), and for increasing a pressure of the second liquid flow (58) in order to obtain the delivered flow (18), the thermal unit (86) being adapted for providing the second heating fluid (92).

3. The installation (10) according to claim 1 or 2, wherein the liquefaction unit (66) is adapted for precooling the pressurized gas flow (64) by a fifth heat exchange with a second cooling fluid (112) prior to the first heat exchange with the first cooling fluid (68), the thermal unit (86) being adapted for providing the second cooling fluid (112).

4. The installation (10) according to claim 3, wherein the pressurized gas flow (64) is at a temperature comprised between 50°C and 90°C before the fifth heat exchange, and at a temperature comprised between 0°C and 20°C after the fifth heat exchange and before the second heat exchange.

5. The installation (10) according to any one of claims 1 to 4, wherein the separation unit (72) comprises a venting system (100) adapted for venting at least part of the second gas flow (76).

6. The installation (10) according to any one of claims claim 1 to 5, wherein the platform (12) comprises: - a purification unit (94) adapted for receiving the second gas flow (76) and a fifth liquid flow (96), and for producing a fourth gas flow (98) and a sixth liquid flow (99), the fifth liquid flow (96) comprising a part of the first liquid flow (56), the second liquid flow (58) comprising the sixth liquid flow (99), a mass flow of CO2 being smaller in the fourth gas flow (98) than in the second gas flow (76), and - a venting system (100) adapted for venting the fourth gas flow (98).

7. The installation (10) according to claim 6, wherein the purification unit (94) comprises a purification column (116), at least part of the fourth gas flow (98) being collected at the top of the purification column (116), at least part of the sixth liquid flow (99) being collected at the bottom of the purification column (116).

8. The installation (10) according to any one of claims 1 to 7, wherein the first heating fluid (82) comprises glycolated water.

9. The installation (10) according to any one of claims 1 to 8, wherein the thermal unit (86) is adapted for recovering the first heating fluid (82) after the second heat exchange from the vaporizing unit (78) in the second operating mode in order to obtain a recovered flow (126), and for heating at least a part (124) of the recovered flow (126) by the third heat exchange in order to obtain a heated flow (128), the first heating fluid (82) comprising at least a part of the heated flow (128).

10. The installation (10) according to claim 9, wherein the thermal unit (86) is adapted for splitting the recovered flow (126) at least into the part (124) intended to be heated by the third heat exchange, and into a second cooling fluid (112), the liquefaction unit (66) being adapted for precooling the pressurized gas flow (64) by heat exchange with the second cooling fluid (112).

11. The installation (10) according to claim 9 or 10, wherein the thermal unit (86) forms a loop (128) comprising a pumping system (130), a make-up tank (132), and a heat exchanger (134) adapted for performing the third heat exchange.

12. The installation (10) according to any one of claims 1 to 11, wherein: - the separation unit (72) comprises a drum (114), and / or - the compression unit (60) comprises a scrubber (104) adapted for scrubbing the first gas flow (62), and at least one compressor (106) adapted for pressurizing the first gas flow (62) after said scrubbing.

13. The installation (10) according to any one of claims 1 to 12, wherein: - the storage unit (50) is designed for receiving the feed (14) at a pressure comprised between 7 and 45 bar absolute, and for delivering the first liquid flow (56) at a pressure comprised between 20 and 70 bar absolute, and / or - the compression unit (60) is designed for obtaining the pressurized gas flow (64) at a pressure comprised between 40 and 80 bar absolute.

14. The installation (10) according to any one of claims 1 to 13, comprising a second platform (20) adapted for injecting the delivered flow (18) underground, for producing power, and for delivering a part (24) of said power to the floating platform (12).

15. A process comprising: - obtaining an installation (10) as described by any one of claims 1 to 14, - intermittently receiving the CO2 rich feed (14) from off-loading ships (16, 17), - delivering the CO2 rich flow (18), - receiving and storing the feed (14) in the storage unit (50), and delivering the first liquid flow (56) from the liquid phase(s) (52), - obtaining the delivered flow (18) using a second liquid flow (58) including at least a part of the first liquid flow (56), - receiving the first gas flow (62) in the compression unit (60) from the storage unit (50) and compressing the first gas flow (62) in order to obtain the pressurized gas flow (64), - at least partly liquefying the pressurized gas flow (64) in the liquefaction unit (66) by the first heat exchange with the first cooling fluid (68) in order to obtain the at least partly liquefied flow (70), - separating the at least partly liquefied flow (70) in the separation unit (72) into the third liquid flow (74) and the second gas flow (76), and receiving the third liquid flow (74) in the storage unit (50), - vaporizing the fourth liquid flow (80) in the vaporizing unit (78) by the second heat exchange with the first heating fluid (82) in order to obtain the third gas flow (84), and receiving the third gas flow (84) in the storage unit (50), - obtaining the first heating fluid (82) from the thermal unit (86), and performing the third heat exchange in the thermal unit (86) with water (88) coming from the body of water (48), and - switching the platform (12) at least between the first operation mode and the second operation mode.

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