Heat management method in a combined process to produce methanol from water and co 2

Abstract

The present disclosure relates to a heat management method in a methanol-generating unit remarkable in that the reactor (100) of the methanol-generating unit comprises a cooling device and wherein the steam (5, 7) recovered from said cooling device has a pressure which is below 0.32 MPa and regulates the thermal energy of the separation unit placed downstream of said methanol-generating unit.

Description

[0001] Heat management method in a combined process to produce methanol from water and CO2

[0002] Field of the disclosure

[0003] The present disclosure relates to a heat management method in a combined process to produce methanol from water and carbon dioxide. More specifically, the present disclosure relates to a heat management method in a methanol-generating unit.

[0004] Technical background

[0005] Methanol is widely used in different applications such as the synthesis of formaldehyde, which is then involved in the manufacture of plastic materials, paints, and textiles, for instance; the production of dimethyl ether, which may be used in aerosols or as an alternative fuel for diesel engines; the transesterification of triglycerides to produce biodiesel; or as a solvent or a fuel for engines.

[0006] Methanol is commercially produced from synthesis gas syngas), namely a mixture of carbon oxides ( / .e., carbon monoxide (CO) and / or carbon dioxide (CO2)) and hydrogen (H2) that can be produced from a variety of carbonated sources.

[0007] CO and CO2react with H2according to the following equations:

[0008] (1 ) CO + 2H2CH3OH

[0009] (2) CO2 + 3H2CH3OH + H2O

[0010] (3) CO + H2O CO2 + H2wherein the third one corresponds to the water-gas shift (WGS) reaction.

[0011] When methanol is produced by a process involving the production of hydrogen by water electrolysis using green electricity over an alkaline electrolyser and its use to convert CO2 in a C02-to-methanol unit, the C02-to-methanol pathway consumes 12.3 kWh / kgMeoH.

[0012] This amount of energy spent on the generation of methanol can be considered as an impediment, since the current trends are rather focusing on processes that are ecological and / or energy-saving, with the ultimate goal of preserving the environment.

[0013] Such an approach implementing green policies has already been executed at some point. For example, the feeding of hydrogen and / or syngas using solid oxide electrolyser cell has succeeded in decreasing the amount of energy needed to perform the required reaction. A solid oxide electrolyser cell allows indeed to achieve the electrolysis of steam (SOEC) or the co-electrolysis of steam and CO2 (co-SOEC) by using a solid oxide electrolyte to produce hydrogen gas or syngas respectively. The use of a high-temperature electrolyser allows using more heat energy than electrical energy. The energy is partially recovered on the SOEC / co- SOEC, as in US 2018 / 0287179, to pre-heat the steam from 125°C-180°C to the electrolysis temperature. The fact of being able to produce steam on the combined process leads reducing the heat energy to provide to the electrolyser and the distillation unit, increasing, therefore, the overall energy efficiency of the process. The solid oxide electrolyser cell usually operates at temperatures which allow high-temperature electrolysis to occur, typically between 500°C and 865°C. Thus, when combined with the water electrolysis, the CC>2-to-methanol pathway is consuming 1 1.59 kWh / kgMeoH and when combined with co-electrolysis of CO2, the CC>2-to- methanol pathway is consuming 10.48 kWh / kgMeoH.

[0014] However, there is still a need to reduce the energy consumption of a methanol-generating process in order to implement the ongoing green environmental policies.

[0015] Summary

[0016] According to a first aspect, the disclosure provides a heat management method in a methanolgenerating unit, said method is remarkable in that it comprises the following steps: a) providing a methanol-generating unit and a separation unit, wherein the separation unit is placed downstream of the methanol-generating unit and is in fluidic connection with it, wherein said separation unit comprises a temperatureregulating device, and wherein said methanol-generating unit comprises one or more reactors each comprising a cooling device; b) operating said at least one reactor under first operating conditions comprising at least regulating the thermal energy of said at least one reactor by adjusting the temperature of the cooling device with water; c) recovering from said cooling device, after said step of regulating the thermal energy, a first stream, said first stream comprising steam at a pressure P1 ; d) decreasing the pressure of said first stream so as to recover a second stream, said second stream comprising steam at a pressure P2, P2 being below 0.32 MPa and wherein P2 < P1 ; e) operating said separation unit under second operating conditions comprising regulating the thermal energy of said separation unit by transferring the thermal energy of the second stream recovered at step (d) to the temperature-regulating device of the separation unit.

[0017] Surprisingly, it has been found to that lowering the pressure of the stream that will be used to transfer its thermal energy to the temperature-regulating device of the separation unit allows to reduce the overall energy consumption of the methanol synthesis. For example, the first operating conditions of step (b) comprise a start-of-run outlet reactor temperature ranging between 200°C and 320°C, preferably between 220°C and 275°C.

[0018] For example, the water used in step (b) for adjusting the temperature of the cooling device has a pressure ranging between 1.5 MPa and 12.0 MPa, or between 2.2 MPa and 7.0 MPa.

[0019] For example, the water used in step (b) for adjusting the temperature of the cooling device has a temperature ranging between 100°C and 200°C, or between 120°C and 150°C.

[0020] For example, the first stream is at a temperature T 1 comprised between 200°C and 325°C, or between 200°C and 300°C, preferably between 205°C and 295°C, more preferably between 210°C and 290°C, even more preferably between 215°C and 285°C, most preferably between 220°C and 280°C, even most preferably between 220°C and 275°C.

[0021] For example, the pressure P1 of the first stream is comprised between 1 .5 MPa and 12.0 MPa, preferably between 2.2 MPa and 7.0 MPa.

[0022] For example, the pressure P1 of the first steam corresponds to the pressure of water used in step (b).

[0023] For example, the pressure P2 of the second stream is below 0.31 MPa, preferably below 0.30 MPa, more preferably below 0.29 MPa, even more preferably below 0.28 MPa, most preferably below 0.27 MPa.

[0024] For example, the pressure P2 of the second stream is ranging between 0.11 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0025] Advantageously, the second stream comprising steam at a pressure P2 further comprises one condensate; and the method further comprises the step of separating the steam from said condensate so as to recover a third stream, said third stream comprising steam at a pressure P3, wherein P3 is equal or inferior to P2.

[0026] With preference, the step of regulating the thermal energy carried out in step (e) is the step of transferring the thermal energy of the third stream to the temperature-regulating device of the separation unit.

[0027] For example, the pressure P3 of the third stream is below 0.31 MPa, preferably below 0.30 MPa, more preferably below 0.29 MPa, even more preferably below 0.28 MPa, most preferably below 0.27 MPa. For example, the pressure P3 of the third stream is ranging between 0.10 MPa and 0.31 MPa, or between 0.1 1 MPa and 0.28 MPa, preferably between 0.12 MPa and 0.27 MPa, more preferably between 0.13 MPa and 0.26 MPa.

[0028] The pressure P1 of the first stream and / or the pressure P3 of the third stream is measured at dew point.

[0029] Electrolysis of water

[0030] Advantageously, in a first embodiment, the method further comprises providing one or more solid oxide electrolyser cells, feeding said one or more solid oxide electrolyser cells with steam, and working said one or more solid oxide electrolyser cells under electrical power at a temperature higher than 400°C so as to generate at least a hydrogen-rich effluent; and in that the first operating conditions used at step (b) further comprises providing a carbon oxides feedstock to said at least one reactor, providing the hydrogen-rich effluent generated by working said one or more solid oxide electrolyser cells as a stream of hydrogen and mixing together the carbon oxides feedstock and the stream of hydrogen within said at least one reactor so as to produce a methanol effluent.

[0031] For example, the method further comprises the step of increasing the pressure of said hydrogen containing-effluent before using it as stream of hydrogen in the first operating conditions used at step (b).

[0032] For example, said hydrogen-rich effluent is at a temperature T2effluent ranging between 130°C and 250°C, preferably between 140°C and 240°C.

[0033] Advantageously, the step of working said one or more solid oxide electrolyser cells under electrical power further generates an oxygen-containing effluent, and the method further comprises the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered at step (c).

[0034] For example, said oxygen-containing effluent is at a temperature TO2effluent ranging between 320°C and 390°C, preferably between 330°C and 380°C.

[0035] With preference, in an embodiment, the step of transferring the thermal energy of the oxygencontaining effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1.29 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a first additional stream of steam, and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said additional stream of steam to the temperatureregulating device of the separation unit.

[0036] For example, the water stream can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1.26 MPa, even more preferably between 0.34 MPa and 1.25 MPa, most preferably between 0.35 MPa and 1.24 MPa. Such water stream is a medium-pressurized water stream.

[0037] With preference, in another embodiment, the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a first additional stream of steam, and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said additional stream of steam to the temperature-regulating device of the separation unit.

[0038] For example, the water stream can be at a pressure below 0.32 MPa, or below 0.30 MPa, preferably below 0.29 MPa, more preferably below 0.28 MPa, even more preferably below 0.27 MPa. For example, the water stream 24 can be at a pressure ranging between 0.10 MPa and 0.30 MPa, preferably between 0.1 1 MPa and 0.29 MPa, more preferably between 0.12 MPa and 0.28 MPa, even more preferably 0.13 MPa and 0.27 MPa. Such water stream 24 is a low-pressurized water stream.

[0039] More preferably, the method further comprises a step of transferring the thermal energy of the hydrogen-rich effluent to the water stream at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen outflow to said water stream so as to generate the first additional stream of steam.

[0040] For example, the step of transferring the thermal energy of said first additional stream of steam to the temperature-regulating device of the separation unit is carried out on a first part of said first additional stream of steam, and a second part of said first additional stream of steam is subjected to a step of pressure increase before being fed to said one or more solid oxide electrolyser cells. For example, the first additional stream of steam is at a pressure ranging between 0.11 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0041] For example, the first additional stream of steam is at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0042] With preference, the step of pressure increase comprises increasing the pressure of the second part of said first additional stream of steam into the range comprised between 0.31 MPa and 1.30 MPa, preferably between 0.32 MPa and 1.29 MPa, more preferably between 0.33 MPa and 1.28 MPa, even more preferably between 0.34 MPa and 1.27 MPa, most preferably between 0.35 MPa and 1.26 MPa, even most preferably between 0.36 MPa and 1.25 MPa.

[0043] With preference, the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1 .29 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a second additional stream of steam, the method further comprises the step of feeding said second additional stream of steam to said one or more solid oxide electrolyser cells.

[0044] For example, the water stream can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1.26 MPa, even more preferably between 0.34 MPa and 1.25 MPa, most preferably between 0.35 MPa and 1.24 MPa. Such water stream is a medium-pressurized water stream.

[0045] Advantageously, the method further comprises a step of transferring the thermal energy of the hydrogen-rich effluent to the water stream at a pressure ranging between 0.32 MPa and 1 .29 MPa before the step of transferring the thermal energy of the oxygen outflow to said water stream so as to generate the second additional stream of steam.

[0046] For example, the second additional stream of steam is at a pressure ranging between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa. For example, the second additional stream of steam is at a temperature ranging between 142°C and 184°C, preferably between 143°C and 180°C, more preferably between 144°C and 175°C.

[0047] Advantageously, the step of working said one or more solid oxide electrolyser cells under electrical power further generates an oxygen-containing effluent; the method further comprises the step of providing a water stream at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen-containing effluent to said water stream so as to generate a third additional stream of steam; and the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of the third additional stream of steam to the temperature-regulating device of the separation unit.

[0048] With preference, the method further comprises a step of transferring the thermal energy of the hydrogen-rich effluent to the water stream at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen-containing effluent to said water stream so as to generate the third additional stream of steam.

[0049] For example, the step of transferring the thermal energy of said third additional stream of steam to the temperature-regulating device of the separation unit is carried out on a first part of said third additional stream of steam, and a second part of said third additional stream of steam is subjected to a step of pressure increase before being fed to said one or more solid oxide electrolyser cells.

[0050] For example, the third additional stream of steam is at a pressure ranging between 0.11 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0051] For example, the third additional stream of steam is at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0052] With preference, the step of pressure increase comprises increasing the pressure of the second part of said third additional stream of steam into the range comprised between 0.31 MPa and 1.30 MPa, preferably between 0.32 MPa and 1.29 MPa, more preferably between 0.33 MPa and 1.28 MPa, even more preferably between 0.34 MPa and 1.27 MPa, most preferably between 0.35 MPa and 1.26 MPa, even most preferably between 0.36 MPa and 1.25 MPa.

[0053] Advantageously, the hydrogen-rich effluent is subjected to a pressure increase step before being directed to the reactor, said pressure increase step generating heat, and the method further comprises the step of providing a water stream and the step of transferring the heat generated by the pressure increase step to said water stream so as to generate a fourth additional stream of steam, said fourth additional stream of steam being then fed to said one or more solid oxide electrolyser cells. With preference, said water stream provided to generate the fourth additional stream of steam is at a pressure ranging between 0.32 MPa and 1.29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa.

[0054] Advantageously, the step (b) of operating said at least one reactor generates a reactor effluent, and the method further comprises the step of providing a water stream and the step of transferring the thermal energy of said reactor effluent to said water stream so as to generate a fifth additional stream of steam, said fifth additional stream of steam being then fed to said one or more solid oxide electrolyser cells. With preference, said water stream provided to generate the fifth additional stream of steam is at a pressure ranging between 0.32 MPa and 1.29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1 .27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa.

[0055] Advantageously, the method of the present disclosure is remarkable in that

[0056] - the step (b) of operating said at least one reactor generates a reactor effluent, and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1.29 MPa, and the step of transferring the thermal energy of said reactor effluent to said water stream so as to generate a fifth additional stream of steam, said fifth additional stream of steam being then fed to said one or more solid oxide electrolyser cells; the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a first additional stream of steam, and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said additional stream of steam to the temperature-regulating device of the separation unit; and the method further comprises a step of transferring the thermal energy of the hydrogen-rich effluent to the water stream at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen outflow to said water stream so as to generate the first additional stream of steam; and

[0057] - the hydrogen-rich effluent is subjected to a pressure increase step before being directed to the reactor, said pressure increase step generating heat, and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1 .29 MPa and the step of transferring the heat generated by the pressure increase step to said water stream so as to generate a fourth additional stream of steam, said fourth additional stream of steam being then fed to said one or more solid oxide electrolyser cells.

[0058] Co-electrolvsis of water and CO2

[0059] Advantageously, in a second embodiment, the method further comprises providing one or more solid oxide electrolyser cells, feeding said one or more solid oxide electrolyser cells with steam and carbon dioxide, and working said one or more solid oxide electrolyser cells under electrical power at a temperature higher than 400°C so as to generate at least a syngas effluent; and in that the first operating conditions used at step (b) further comprises providing the syngas effluent generated by working said one or more solid oxide electrolyser cells so as to produce a methanol effluent. Optionally, a carbon oxides feedstock can be also be provided to said at least one reactor.

[0060] For example, the method further comprises the step of increasing the pressure of said syngas effluent before using it as stream of hydrogen in the first operating conditions used at step (b).

[0061] For example, the step of feeding said one or more solid oxide electrolyser cells with steam and carbon dioxide further comprises feeding said solid oxide electrolyser with hydrogen, syngas, methane, hydrocarbons or a mixture thereof. For example, hydrocarbons are alkanes.

[0062] For example, the syngas effluent comprises hydrogen, CO2 and CO. With preference, the molar ratio between CO and CO2 is superior to 1 .

[0063] For example, said syngas effluent is at a temperature Tsyngas effluent ranging between 130°C and 250°C, preferably between 140°C and 240°C.

[0064] Advantageously, the step of working said one or more solid oxide electrolyser cells under electrical power further generates an oxygen-containing effluent, and the method further comprises the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered at step (c). With preference, the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a first additional stream of steam, and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said first additional stream of steam to the temperature-regulating device of the separation unit.

[0065] For example, the water stream can be at a pressure below 0.32 MPa, or below 0.30 MPa, preferably below 0.29 MPa, more preferably below 0.28 MPa, even more preferably below 0.27 MPa. For example, the water stream 24 can be at a pressure ranging between 0.10 MPa and 0.30 MPa, preferably between 0.1 1 MPa and 0.29 MPa, more preferably between 0.12 MPa and 0.28 MPa, even more preferably 0.13 MPa and 0.27 MPa. Such water stream 24 is a low-pressurized water stream.

[0066] More preferably, the method further comprises a step of transferring the thermal energy of the syngas effluent to the water stream at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen outflow to said water stream so as to generate the first additional stream of steam.

[0067] For example, the step of transferring the thermal energy of said first additional stream of steam to the temperature-regulating device of the separation unit is carried out on a first part of said first additional stream of steam, and a second part of said first additional stream of steam is subjected to a step of pressure increase before being fed to said one or more solid oxide electrolyser cells.

[0068] For example, the first additional stream of steam is at a pressure ranging between 0.11 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0069] For example, the first additional stream of steam is at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0070] With preference, the step of pressure increase comprises increasing the pressure of the second part of said first additional stream of steam into the range comprised between 0.31 MPa and 1.30 MPa, preferably between 0.32 MPa and 1.29 MPa, more preferably between 0.33 MPa and 1.28 MPa, even more preferably between 0.34 MPa and 1.27 MPa, most preferably between 0.35 MPa and 1.26 MPa, even most preferably between 0.36 MPa and 1.25 MPa.

[0071] With preference, the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1 .29 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a second additional stream of steam, the method further comprises the step of feeding said second additional stream of steam to said one or more solid oxide electrolyser cells.

[0072] For example, the water stream can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1.26 MPa, even more preferably between 0.34 MPa and 1.25 MPa, most preferably between 0.35 MPa and 1.24 MPa. Such water stream is a medium-pressurized water stream.

[0073] Advantageously, the method further comprises a step of transferring the thermal energy of the syngas effluent to the water stream at a pressure ranging between 0.32 MPa and 1 .29 MPa before the step of transferring the thermal energy of the oxygen outflow to said water stream so as to generate the second additional stream of steam.

[0074] For example, the second additional stream of steam is at a pressure ranging between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa.

[0075] For example, the second additional stream of steam is at a temperature ranging between 142°C and 184°C, preferably between 143°C and 180°C, more preferably between 144°C and 175°C.

[0076] Advantageously, the step of working said one or more solid oxide electrolyser cells under electrical power further generates an oxygen-containing effluent; the method further comprises the step of providing a water stream at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen-containing effluent to said water stream so as to generate a third additional stream of steam; and the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of the third additional stream of steam to the temperature-regulating device of the separation unit. With preference, the method further comprises a step of transferring the thermal energy of the syngas effluent to the water stream at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen-containing effluent to said water stream so as to generate the third additional stream of steam.

[0077] For example, the step of transferring the thermal energy of said third additional stream of steam to the temperature-regulating device of the separation unit is carried out on a first part of said third additional stream of steam, and a second part of said third additional stream of steam is subjected to a step of pressure increase before being fed to said one or more solid oxide electrolyser cells.

[0078] For example, the third additional stream of steam is at a pressure ranging between 0.11 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0079] For example, the third additional stream of steam is at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0080] With preference, the step of pressure increase comprises increasing the pressure of the second part of said third additional stream of steam into the range comprised between 0.31 MPa and 1.30 MPa, preferably between 0.32 MPa and 1.29 MPa, more preferably between 0.33 MPa and 1.28 MPa, even more preferably between 0.34 MPa and 1.27 MPa, most preferably between 0.35 MPa and 1.26 MPa, even most preferably between 0.36 MPa and 1.25 MPa.

[0081] Advantageously, the syngas effluent is subjected to a pressure increase step before being directed to the reactor, said pressure increase step generating heat, and the method further comprises the step of providing a water stream and the step of transferring the heat generated by the pressure increase step to said water stream so as to generate a fourth additional stream of steam, said fourth additional stream of steam being then fed to said one or more solid oxide electrolyser cells. With preference, said water stream provided to generate the fourth additional stream of steam is at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1.26 MPa, even more preferably between 0.34 MPa and 1.25 MPa, most preferably between 0.35 MPa and 1 .24 MPa.

[0082] Advantageously, the step (b) of operating said at least one reactor generates a reactor effluent, and the method further comprises the step of providing a water stream and the step of transferring the thermal energy of said reactor effluent to said water stream so as to generate a fifth additional stream of steam, said fifth additional stream of steam being then fed to said one or more solid oxide electrolyser cells. With preference, said water stream provided to generate the fifth additional stream of steam is at a pressure ranging between 0.32 MPa and 1.29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1 .27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa.

[0083] Advantageously, the method of the present disclosure is remarkable in that

[0084] - the step (b) of operating said at least one reactor generates a reactor effluent, and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1.29 MPa, and the step of transferring the thermal energy of said reactor effluent to said water stream so as to generate a fifth additional stream of steam, said fifth additional stream of steam being then fed to said one or more solid oxide electrolyser cells; the step of transferring the thermal energy of the oxygen-containing effluent to the first stream recovered in step (c) generates an oxygen outflow; and the method further comprises the step of providing a water stream at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen outflow to said water stream so as to generate a first additional stream of steam, and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said additional stream of steam to the temperature-regulating device of the separation unit; and the method further comprises a step of transferring the thermal energy of the syngas effluent to the water stream at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen outflow to said water stream so as to generate the first additional stream of steam; and

[0085] - the syngas effluent is subjected to a pressure increase step before being directed to the reactor, said pressure increase step generating heat, and the method further comprises the step of providing a water stream at a pressure ranging between 0.32 MPa and 1.29 MPa and the step of transferring the heat generated by the pressure increase step to said water stream so as to generate a fourth additional stream of steam, said fourth additional stream of steam being then fed to said one or more solid oxide electrolyser cells. Whichever the embodiment selected, the heat management method can be further described as one or more of the following:

[0086] - The step (d) of decreasing the pressure of said first stream further produces electrical energy; and the method further comprises the step of supplying said electrical energy to said one or more solid oxide electrolyser cells so as to run said one or more solid oxide electrolyser cells.

[0087] - The methanol-generating unit provided at step (a) comprises one or more first compressors, and the step (d) of decreasing the pressure of said first stream further produces electrical energy and / or shaft work; and the method further comprises the step of supplying said electrical energy and / or shaft work to said one or more first compressors so as to run the one or more first compressors comprised within the methanol-generating unit.

[0088] - Said oxygen-containing effluent is at a temperature TO2effluent ranging between 300°C and 400°C, preferably between 305°C and 395°C, more preferably between 310°C and 390°C.

[0089] - Said oxygen outflow is at a temperature TO2outflow ranging between 260°C and 360°C, preferably between 265°C and 355°C, more preferably between 270°C and 350°C.

[0090] According to a second aspect, the disclosure provides an installation for producing methanol remarkable in that the installation comprising

[0091] - a methanol-generating unit and a separation unit, wherein said separation unit is placed downstream of the methanol-generating unit and is in fluidic connection with it, wherein the separation unit comprises a temperature-regulating device, and wherein the methanol-generating unit comprising one or more reactors, each reactor comprising a cooling device;

[0092] - at least one steam pressure-reducing device, the steam pressure-reducing device being placed downstream of said cooling device and upstream of said temperatureregulating device;

[0093] - a first line connecting fluidically the cooling device to the one or more steam pressurereducing devices;

[0094] - a second line connecting fluidically the one or more steam pressure-reducing devices to the temperature-regulating device, and wherein the one or more steam pressurereducing devices comprise at least one steam pressure regulator.

[0095] For example, the one or more steam pressure regulators are one or more pressure control valves. For example, one steam pressure-reducing device is at least one turbine.

[0096] Advantageously, the installation further comprises a gas-liquid separator, said gas-liquid separator being placed on the second line downstream of and in fluidic connection with said at least one steam pressure-reducing device, said gas-liquid separator comprising an overhead fluidically connected to the temperature-regulating device.

[0097] Advantageously, the installation further comprises one or more solid oxide electrolyser cells, each of said one or more solid oxide electrolyser cells comprising a hydrogen-output line to direct a hydrogen-rich effluent or a syngas effluent out of said solid oxide electrolyser cell.

[0098] Advantageously, the installation further comprises one or more solid oxide electrolyser cells, each of said one or more solid oxide electrolyser cells comprising a hydrogen-output line to direct a hydrogen-rich effluent or a syngas effluent out of said solid oxide electrolyser cell; and wherein the installation further comprises a line fluidically connecting the hydrogen-output line to the one or more reactors of the methanol-generating unit.

[0099] Description of the figures

[0100] Figure 1 a: Installation comprising a methanol-generating unit upstream of a separation unit along with a solid oxide electrolyser cell working in electrolysis mode (SOEC).

[0101] Figure 1 b: Installation comprising a methanol-generating unit upstream of a separation unit along with a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC).

[0102] Figure 2a: Installation comprising a methanol-generating unit upstream of a separation unit. Steam at medium pressure ( / .e., above 0.32 MPa) is directed from a steam pressure-reducing device to the separation unit. A solid oxide electrolyser cell working in electrolysis mode (SOEC) is shown.

[0103] Figure 2b: Installation comprising a methanol-generating unit upstream of a separation unit. Steam at medium pressure ( / .e., above 0.32 MPa) is directed from a steam pressure-reducing device to the separation unit. A solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) is shown.

[0104] Figure 3a: Installation according to the present disclosure comprising a methanol-generating unit upstream of a separation unit. Steam at low pressure ( / .e., below 0.32 MPa) is directed from a steam pressure-reducing device to the separation unit. A solid oxide electrolyser cell working in electrolysis mode (SOEC) is shown. Figure 3b: Installation according to the present disclosure comprising a methanol-generating unit upstream of a separation unit. Steam at low pressure ( / .e., below 0.30 MPa) is directed from a steam pressure-reducing device to the separation unit. A solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) is shown.

[0105] Figure 4a: Installation according to the present disclosure benefiting from an oxygencontaining effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) to pre-heat a stream of steam entering a steam pressure-reducing device.

[0106] Figure 4b: Installation according to the present disclosure benefiting from an oxygencontaining effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co- SOEC) to pre-heat a stream of steam entering a steam pressure-reducing device.

[0107] Figure 5a: Installation according to the present disclosure benefiting from an oxygencontaining effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressure-reducing device is used to heat the steam directed to the separation unit.

[0108] Figure 5b: Installation according to the present disclosure benefiting from an oxygencontaining effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co- SOEC) to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressurereducing device is used to heat the steam directed to the separation unit.

[0109] Figure 6a: Installation according to the present disclosure benefiting from an oxygencontaining effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) to pre-heat a stream of steam entering a steam-pressure reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressure-reducing device is used to heat the steam directed to the separation unit. The hydrogen-rich effluent exiting the solid oxide electrolyser cell is also used to bring the thermal energy required for the steam directed to the separation unit.

[0110] Figure 6b: Installation according to the present disclosure benefiting from an oxygencontaining effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co- SOEC) to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressurereducing device is used to heat the steam directed to the separation unit. The syngas effluent exiting the solid oxide electrolyser cell is also used to bring the thermal energy required for the steam directed to the separation unit.

[0111] Figure 7a: Installation according to the present disclosure wherein an oxygen-containing effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) is used to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressure-reducing device is used to heat the steam that is fed to said solid oxide electrolyser cell.

[0112] Figure 7b: Installation according to the present disclosure wherein an oxygen-containing effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) is used to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the steam stream of steam entering the pressurereducing device is used to heat the steam that is fed to said solid oxide electrolyser cell.

[0113] Figure 8a: Installation according to the present disclosure wherein an oxygen-containing effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) is used to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressure-reducing device is used to heat the steam that is fed to said solid oxide electrolyser cell. The hydrogenrich effluent exiting the solid oxide electrolyser cell is also used to bring the thermal energy required for the steam that is fed to said solid oxide electrolyser cell.

[0114] Figure 8b: Installation according to the present disclosure wherein an oxygen-containing effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) is used to pre-heat a stream of steam entering a steam pressure-reducing device. An oxygen outflow generated from the pre-heating of the stream of steam entering the steam pressurereducing device is used to heat the steam that is fed to said solid oxide electrolyser cell. The syngas effluent exiting the solid oxide electrolyser cell is also used to bring the thermal energy required for the steam that is fed to said solid oxide electrolyser cell.

[0115] Figure 9a: Installation according to the present disclosure wherein an oxygen-containing effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) is used to produce steam that is directed to the separation unit.

[0116] Figure 9b: Installation according to the present disclosure wherein an oxygen-containing effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) is used to produce steam that is directed to the separation unit. Figure 10a: Installation according to the present disclosure wherein an oxygen-containing effluent and a hydrogen-rich effluent exiting a solid oxide electrolyser cell working in electrolysis mode (SOEC) are used to produce steam that is directed to the separation unit.

[0117] Figure 10b: Installation according to the present disclosure wherein an oxygen-containing effluent and a syngas effluent exiting a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) are used to produce steam that is directed to the separation unit.

[0118] Figure 11 a: Installation according to the present disclosure comprising a methanol-generating unit upstream of a separation unit. Steam at low pressure ( / .e., below 0.32 MPa) is directed from a steam pressure-reducing device to the separation unit. A first compressor is upstream to the reactor of the methanol-generating unit and generates heat upon pressure increase of the hydrogen-rich effluent, said heat serving to produce steam fed to a solid oxide electrolyser cell working in electrolysis mode (SOEC).

[0119] Figure 11 b: Installation according to the present disclosure comprising a methanol-generating unit upstream of a separation unit. Steam at low pressure ( / .e., below 0.32 MPa) is directed from a steam pressure-reducing device to the separation unit. A first compressor is upstream to the reactor of the methanol-generating unit and generates heat upon pressure increase of the syngas effluent, said heat serving to produce steam fed to a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC).

[0120] Detailed description

[0121] For the purpose of the disclosure, the following definitions are given.

[0122] The terms "comprising", "comprises" and "comprised of" as used herein are synonymous with "including", "includes" or "containing", "contains", and are inclusive or open-ended and do not exclude additional, non-recited members, elements or method steps. The terms "comprising", "comprises" and "comprised of" also include the term “consisting of”.

[0123] The recitation of numerical ranges by endpoints includes all integer numbers and, where appropriate, fractions subsumed within that range (e.g., 1 to 5 includes 1 , 2, 3, 4, 5 when referring to, for example, a number of elements, and can also include 1.5, 2, 2.75 and 3.80, when referring to, for example, measurements). The recitation of endpoints also includes the recited endpoint values themselves e.g., from 1.0 to 5.0 includes both 1.0 and 5.0). Any numerical range recited herein is intended to include all sub-ranges subsumed therein.

[0124] The reference throughout this specification to “one embodiment” or “an embodiment” means that a particular feature, structure or characteristic described in connection with the embodiment is included in at least one embodiment of the present disclosure. The particular features, structures, characteristics or embodiments may be combined in any suitable manner, as would be apparent to a person skilled in the art from this disclosure, in one or more embodiments. Furthermore, while some embodiments described herein include some but not other features included in other embodiments, combinations of features of different embodiments are meant to be within the scope of the disclosure and form different embodiments, as would be understood by those in the art.

[0125] The unit “kilowatt hours per kilogram of methanol” (kWh / kgMeon) is the reference unit used to measure or indicate the density of energy contained or storable in methanol.

[0126] The value “0 barg” (relative pressure) corresponds to difference of pressure with respect to the atmospheric pressure. Therefore, 0 barg = 1 atm = 101325 Pa (absolute pressure, namely the pressure measured with respect to the vacuum) or 0.101325 MPa, rounded to 0.1 MPa.

[0127] The consumption gain in the methanol production have been simulated using the software ProSimPlus.

[0128] The installations represented at figures 1a and 1 b schematized a methanol-generating unit which is upstream of a separation unit and in fluidic connection with it. The methanolgenerating unit comprises one reactor 100 which is for example in fluidic connection with the separation unit. Indeed, there is a fluidic connection between the reactor 100 and the separation unit, in particular with the distillation column 200. This line conveys the reactor effluent 150 from the reactor 100 to the separation unit. Each reactor comprises a cooling device. The separation unit, such as one or more distillation columns 200, preferably three distillations columns that can be arranged in series, comprises a temperature-regulating device 250. The installation further comprises at least one steam pressure-reducing device, for example a turbine 300. The one or more steam pressure-reducing devices are placed downstream of the cooling device and upstream of the temperature-regulating device. The methanol-generating unit and the separation unit are in combination with one or more solid oxide electrolyser cells 400 which work either in electrolysis mode (figure 1a) or in coelectrolysis mode (figure 1 b). The steam pressure-reducing device comprises at least one steam pressure regulator, which can be one or more pressure control valves (PCV) which are used to reduce the pressure of first stream 3 exiting the cooling device. Upon the pressure reduction of the first stream 3, the steam pressure-reducing device produces electricity and / or shaft work, as schematized by the arrow 9. The second stream 5 exiting the steam pressurereducing device can be therefore used to regulate the thermal energy of the separation unit. The condensate that is the liquid formed when the pressure of a condensable gas is reduced due to (partial) condensation of the gas itself, and that is present into the first stream 3, is optionally removed through a gas / liquid separation column 500, so that a third stream 7 is recovered and a stream 8 comprising the condensate is also recovered. The third stream 7 can also be used to regulate the thermal energy of the separation unit. A complementary stream of steam 11 can be supplemented to the second stream 5 and / or to the third stream 7.

[0129] In the installation represented at figure 2a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.5 MPa and when a one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) is coupled to the methanol-generating unit and to the separation unit, the process of methanol production is consuming 10.98 kWh / kgMeoH.

[0130] In the installation represented at figure 2b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.5 MPa and when a one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) is coupled to the methanol-generating unit and to the separation unit, the process of methanol production is consuming 10.26 kWh / kgMeoH.

[0131] Steam at low pressure (l.e., below 0.32 MPa) from steam pressure-reducing device to separation unit

[0132] As represented at figures 3a and 3b, the present disclosure provides a heat management method in a methanol-generating unit, said method is remarkable in that it comprises the following steps: a) providing a methanol-generating unit and a separation unit, wherein the separation unit is placed downstream of the methanol-generating unit and is in fluidic connection with it, wherein said separation unit comprises a temperatureregulating device 250, and wherein said methanol-generating unit comprises one or more reactors 100 each comprising a cooling device; b) operating said reactor 100 under first operating conditions, said first operating conditions comprising at least regulating the thermal energy of said at least one reactor 100; wherein the step of regulating the thermal energy comprises adjusting the temperature of the cooling device with water 1. This step of adjusting the temperature of the cooling device amounts to adjusting the temperature of the reactor 100. c) recovering from said cooling device, after said step of regulating the thermal energy, a first stream 3, said first stream 3 comprising steam at a pressure P1 ; d) decreasing the pressure of said first stream 3 so as to recover a second stream 5, said second stream 5 comprising steam at a pressure P2, P2 being below 0.32 MPa and wherein P2 < P1 ; e) operating said separation unit under second operating conditions, said second operating conditions comprising regulating the thermal energy of said separation unit; wherein the step of regulating the thermal energy comprises transferring the thermal energy of at least the second stream 5 recovered at step (d) to the temperature-regulating device 250 of the separation unit.

[0133] The heat management method described above is advantageously carried out in an installation for producing methanol remarkable in that the installation comprises:

[0134] - a methanol-generating unit and a separation unit, wherein said separation unit is placed downstream of the methanol-generating unit and is in fluidic connection with it, wherein the separation unit comprises a temperature-regulating device 250, and wherein the methanol-generating unit comprising one or more reactors 100, each reactor 100 comprising a cooling device;

[0135] - at least one steam pressure-reducing device, the steam pressure-reducing device being placed downstream of said cooling device and upstream of said temperatureregulating device 250;

[0136] - a first line connecting fluidically the cooling device to the one or more steam pressurereducing devices;

[0137] - a second line connecting fluidically the one or more steam pressure-reducing devices to the temperature-regulating device, and wherein the one or more steam pressurereducing devices comprise at least one steam pressure regulator.

[0138] For example, the one or more steam pressure regulators are one or more pressure control valves.

[0139] For example, the steam pressure-reducing device is at least one turbine or at least one Venturi scrubber, preferably at least one turbine.

[0140] For example, the first operating conditions of step (b) comprises feeding said at least one reactor 100 with either a carbon oxides feedstock and a hydrogen-rich effluent 15 or a syngas effluent 19 when one or more solid oxide electrolyser cells are provided.

[0141] For example, the carbon oxides of the carbon oxides feedstock provided to said at least one reactor are selected from CO2 and / or CO.

[0142] Advantageously, the pressure of the stream of hydrogen in the first operating conditions used in step (b) can be ranging between 0.1 MPa and 12.0 MPa, preferably between 0.5 MPa, and 9.5 MPa, more preferably between 1.0 MPa and 9.0 MPa; even more preferably between 1.5 MPa and 8.5 MPa, most preferably between 2.0 MPa and 8.0 MPa. Advantageously, the pressure of the carbon oxides feedstock in the first operating conditions used in step (b) is ranging between 0.1 MPa and 12.0 MPa, preferably between 0.5 MPa, and 9.5 MPa, more preferably between 1.0 MPa and 9.0 MPa; even more preferably between 1.5 MPa and 8.5 MPa, most preferably between 2.0 MPa and 8.0 MPa. Similarly, the pressure of a syngas stream in the first operating conditions has the same values, namely it ranges between 0.1 MPa and 12.0 MPa, preferably between 0.5 MPa, and 9.5 MPa, more preferably between 1.0 MPa and 9.0 MPa; even more preferably between 1.5 MPa and 8.5 MPa, most preferably between 2.0 MPa and 8.0 MPa.

[0143] For example, the first operating conditions of step (b) comprise a start-of-run outlet reactor temperature ranging between 200°C and 320°C, preferably between 220°C and 275°C.

[0144] For example, the water 1 used in step (b) for adjusting the temperature of the cooling device has a pressure ranging between 1 .5 MPa and 12.0 MPa, or between 2.2 MPa and 7.0 MPa.

[0145] For example, the water 1 used in step (b) for adjusting the temperature of the cooling device has a temperature ranging between 100°C and 200°C, or between 120°C and 150°C.

[0146] For example, the first stream 3 is at a temperature T 1 comprised between 200°C and 325°C, or between 200°C and 300°C, preferably between 205°C and 295°C, more preferably between 210°C and 290°C, even more preferably between 215°C and 285°C, most preferably between 220°C and 280°C, even most preferably between 220°C and 275°C.

[0147] For example, the pressure P1 of the first stream 3 is comprised between 1.5 MPa and 12.0 MPa, preferably between 2.2 MPa and 7.0 MPa. The pressure P1 of the first stream 3 is measured at dew point.

[0148] For example, the pressure P2 of the second stream 5 is below 0.31 MPa, preferably below 0.30 MPa, more preferably below 0.29 MPa, even more preferably below 0.28 MPa, most preferably below 0.27 MPa.

[0149] For example, the pressure P2 of the second stream 5 is ranging between 0.11 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0150] The step (d) of decreasing the pressure of said first stream further produces electrical energy. Thus, when electrical energy is produced, the method can further comprise the step of supplying said electrical energy to said one or more solid oxide electrolyser cells so as to run said one or more solid oxide electrolyser cells.

[0151] As the methanol-generating unit provided at step (a) comprises one or more first compressors, and the step (d) of decreasing the pressure of said first stream further produces electrical energy and / or shaft work; the method can further comprise the step of supplying said electrical energy and / or shaft work to said one or more first compressors so as to run the one or more first compressors comprised within the methanol-generating unit.

[0152] The second stream 5 comprising steam at a pressure P2 can further comprise a condensate; and the method further advantageously comprises the step of separating the steam from said condensate so as to recover a third stream 7, said third stream 7 comprising steam at a pressure P3, wherein P3 is equal or inferior to P2. A stream 8 comprising a condensate is also recovered. Thus, advantageously, the installation can further comprise a gas-liquid separator 500, said gas-liquid separator 500 being placed on the second line downstream of and in fluidic connection with said at least one steam pressure-reducing device, said gas-liquid separator 500 comprising an overhead fluidically connected to the temperature-regulating device 250.

[0153] With preference, the step of regulating the thermal energy carried out in step (e) is the step of transferring the thermal energy of the third stream 7 to the temperature-regulating device of the separation unit. For example, the pressure P3 of the third stream 7 is below 0.31 MPa, preferably below 0.30 MPa, more preferably below 0.29 MPa, even more preferably below 0.28 MPa, most preferably below 0.27 MPa, even most preferably below 0.26 MPa. For example, the pressure P3 of the third stream 7 is ranging between 0.10 MPa and 0.31 MPa, or between 0.1 1 MPa and 0.28 MPa, preferably between 0.12 MPa and 0.27 MPa, more preferably between 0.13 MPa and 0.26 MPa. The pressure P3 of the third stream 7 is measured at dew point.

[0154] The pressure P1 of the first stream and / or the pressure P3 of the third stream is measured at dew point. The pressure P2 of the second stream is not measured at dew point because it is related to a steam that is at the exit of the steam pressure-reducing device and which subsequently comprises a condensate.

[0155] In the installation represented at figure 3a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) are coupled to the methanol-generating unit and to the separation unit, the process of methanol production is consuming at most 11.05 kWh / kgMeoH, preferably at most 1 1 .00 kWh / kgMeoH.

[0156] In the installation represented at figure 3b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) are coupled to the methanol-generating unit and to the separation unit, the process of methanol production is consuming at most 10.30 kWh / kgMeoH, preferably at most 10.25 kWh / kgMeoH.

[0157] In essence, the present disclosure relates therefore to a heat management method in a methanol-generating unit remarkable in that the reactor 100 of the methanol-generating unit comprises a cooling device and wherein the second and / or third stream comprising steam (5, 7) recovered from said cooling device has a pressure which is below 0.32 MPa and regulates the thermal energy of the corresponding separation unit of the said methanol-generating unit.

[0158] Further improvement by preheating steam before pressure-reducing device thanks to one or more solid oxide electrolvser cells and their oxygen-containing effluent

[0159] Advantageously, and as represented at figures 4a and 4b, the installation further comprises one or more solid oxide electrolyser cells 400, each of said one or more solid oxide electrolyser cells 400 comprising a hydrogen- output line to direct a hydrogen-rich effluent 15 or a syngas effluent 19 out of said solid oxide electrolyser cell 400. With preference, the installation further comprises a line fluidically connecting the hydrogen-output line to the one or more reactors 100 of the methanol-generating unit. With preference, the installation further comprises a hydrogen compression device located on the line fluidically connecting the hydrogen-output line to the one or more reactors 100 of the methanol-generating unit. Therefore, the method can further comprise the step of increasing the pressure of said hydrogen-rich effluent 15 or said syngas effluent 19 before using it in the first operating conditions used at step (b).

[0160] The presence of one or more solid oxide electrolyser cells 400, operating either in electrolysis mode or in co-electrolysis mode, can be further used to enhance the methanol production.

[0161] The one or more solid oxide electrolyser cells have each an anode and a cathode and comprise a solid oxide electrolyte between the anode and the cathode. The anode, the cathode and the solid oxide electrolyte are each composed of one or more ceramic materials. The temperature at which said one or more solid oxide electrolyser cells are working under electrical power can be higher than 425°C, preferably higher than 450°C, more preferably higher than 475°C, even more preferably higher than 500°C. For example, the temperature at which said one or more solid oxide electrolyser cells are working under electrical power is ranging between 400°C and 1000°C, or between 450°C and 900°C, preferably between 500°C and 890°C, more preferably between 550°C and 880°C, even more preferably between 600°C and 870°C, most preferably between 700°C and 860°C.

[0162] For example, the one or more solid oxide electrolyser cells are operated at a current density that is ranging between 0.2 A / cm2and 5 A / cm2, preferably between 0.4 A / cm2and 4.8 A / cm2 For example, the one or more solid oxide electrolyser cells are operated at an electrical potential ranging between 0.2 V / cell and 2.0 V / cell, preferably between 0.4 V / cell and 1.8 V / cell.

[0163] Thus, in a first embodiment, dedicated to the electrolysis mode (SOEC), the one or more solid oxide electrolyser cells 400 are fed with steam 12 and is worked under electrical power at a temperature higher than 400°C so as to generate at least a hydrogen-rich effluent 15.

[0164] For example, the hydrogen-rich effluent 15 comprises at least 50 vol.% of hydrogen based on the total volume of said effluent; preferably at least 60 vol.%, more preferably at least 70 vol.%, even more preferably at least 80 vol.%, most preferably at least 90 vol.%, even most preferably at least 99 vol.%.

[0165] In an alternative second embodiment, dedicated to the co-electrolysis mode (co-SOEC), the one or more solid oxide electrolyser cells 400 are fed with steam 12 and carbon dioxide 17 and is worked under electrical power at a temperature higher than 400°C so as to generate at least a syngas effluent 19.

[0166] For example, the syngas effluent 19 comprises carbon monoxide, hydrogen, carbon dioxide and optionally methane. With preference, the syngas effluent comprises between 15 vol.% and 40 vol.% of carbon monoxide (CO), between 25 vol.% and 35 vol.% of hydrogen (H2), between 2 vol.% and 15 vol.% of carbon dioxide (CO2), and between 0 vol.% and 5 vol.% of methane (CH4) all based on the total volume of said effluent. Indeed, for example, the syngas effluent comprises between 15 vol.% and 40 vol.% of carbon monoxide (CO) based on the total volume of said effluent. For example, the syngas effluent comprises between 25 vol.% and 35 vol.% of hydrogen (H2) based on the total volume of said effluent. For example, the syngas effluent comprises between 2 vol.% and 15 vol.% of carbon dioxide (CO2) based on the total volume of said effluent. For example, the syngas effluent comprises between 0 vol.% and 5 vol.% of methane (CH4) based on the total volume of said effluent.

[0167] Advantageously, in either the first or the second embodiment, the first operating conditions used at step (b) further comprises providing a carbon oxides feedstock to said at least one reactor 100, providing respectively the hydrogen-rich effluent 15 or the syngas effluent 19 generated by working said one or more solid oxide electrolyser cells 400 as a stream of hydrogen and mixing together the carbon oxides feedstock and the stream of hydrogen within said at least one reactor 100 so as to produce a methanol effluent. With preference, the method further comprises the step of increasing the pressure of said hydrogen-rich effluent 15 or of said syngas effluent 19 before using it as stream of hydrogen in the first operating conditions used at step (b).

[0168] For example, said hydrogen-rich effluent 15 or said syngas effluent 19 is at a temperature T 2 effluent ranging between 130°C and 250°C, preferably between 140°C and 240°C.

[0169] Advantageously, a first stream 3 of steam is circulating within the first line from the cooling device to the one or more steam pressure-reducing devices, and the installation further comprises one or more solid oxide electrolyser cells 400, each of said one or more solid oxide electrolyser cells 400 comprising an oxygen-output line to direct an oxygen-containing effluent 13 out of said solid oxide electrolyser cell 400; and wherein the installation further comprises a first heat exchanger placed on the first line, the oxygen-output line being connected with said first heat exchanger so that the thermal energy of the oxygen-containing effluent 13 is transferred to the first stream 3 of steam circulating within the first line.

[0170] Thus, in the heat management method of the present disclosure, the step of working said one or more solid oxide electrolyser cells 400 under electrical power further generates an oxygencontaining effluent 13, and the method can further comprise the step of transferring the thermal energy of the oxygen-containing effluent 13 to the first stream 3 recovered at step (c). The stream entering the steam pressure-reducing device, such as the turbine 300, is thus preheated thanks to the thermal energy of the oxygen-containing effluent 13.

[0171] The oxygen-containing effluent 13 can be at a temperature TO2effluent ranging between 320°C and 390°C, preferably between 330°C and 380°C, more preferably between 340°C and 370°C.

[0172] In the installation represented at figure 4a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the thermal energy of the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) is transferred to the first stream 3, the process of methanol production is consuming at most 1 1 .00 kWh / kgMeoH, preferably at most 10.95 kWh / kgMeoH.

[0173] In the installation represented at figure 4b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the thermal energy of the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) is transferred to the first stream 3, the process of methanol production is consuming at most 10.25 kWh / kgMeoH, preferably at most 10.20 kWh / kgMeoH.

[0174] Further improvement by production of steam to improve the efficacy of the separation unit With preference, the installation further comprises a water supply upstream of a second heat exchanger, and a water line directing a water stream 23 for example at a pressure ranging between 0.32 MPa and 1.29 MPa, from said water supply to said second heat exchanger, wherein the installation further comprises a third line connecting the first heat exchanger with the second heat exchanger to direct an oxygen outflow 21 from said first heat exchanger to said second heat exchanger, so that the thermal energy of the oxygen outflow 21 is transferred to the water stream 23 directed into the water line to produce a first additional steam 25 of steam that is directed into an additional line connecting the second heat exchanger to the temperature-regulating device 250.

[0175] For example, the water stream 23 can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa. Such water stream 23 is a medium-pressurized water stream.

[0176] Thus, the step of transferring the thermal energy of the oxygen-containing effluent 13 to the first stream 3 recovered in step (c) generates an oxygen outflow 21 ; and the method can further comprise the step of providing a water stream 23 for example, at a pressure ranging between 0.32 MPa and 1 .29 MPa and the step of transferring the thermal energy of at least the oxygen outflow 21 to said water stream 23 so as to generate a first additional stream of steam 25, and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said first additional stream of steam 25 to the temperatureregulating device of the separation unit.

[0177] For example, in that case wherein one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) are implied, the first additional stream of steam 25 is at a pressure ranging between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1 .00 MPa, more preferably between 0.40 MPa and 0.90 MPa. For example, in that case wherein one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) are implied, the first additional stream of steam 25 is at a temperature ranging between 142°C and 184°C, preferably between 143°C and 180°C, more preferably between 144°C and 175°C.

[0178] The oxygen outflow can be at a temperature TO2outflow ranging between 280°C and 350°C, preferably between 290°C and 340°C, more preferably between 300°C and 330°C.

[0179] This is implemented in the installation represented at figures 5a. It is noted that in the case where the oxygen-containing effluent 13 is exiting the one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) (case of figure 5b), the water stream 24 which is provided is for example at a pressure below 0.32 MPa, and the step of transferring the thermal energy of the first additional stream of steam 25 to the temperature-regulating device of the separation unit is carried out on a first part 27 of said first additional stream of steam, and a second part 29 of said first additional stream of steam is subjected to a step of pressure increase, for example by directing said second part 29 of the first additional stream of steam into a second compressor 600 before being fed to said one or more solid oxide electrolyser cells 400. Indeed, the transfer of the thermal energy of the oxygen outflow 21 to the water stream 24 at a pressure below 0.32 MPa generates a first additional stream of steam 25 at pressure of at most 0.32 MPa, which provides an excess of the steam, namely the second part 29 of the first additional stream of steam that can thus be reused to feed the one or more solid oxide electrolyser cells 400.

[0180] For example, the water stream 24 can be at a pressure below 0.32 MPa, or below 0.30 MPa, preferably below 0.29 MPa, more preferably below 0.28 MPa, even more preferably below 0.27 MPa. For example, the water stream 24 can be at a pressure ranging between 0.10 MPa and 0.30 MPa, preferably between 0.1 1 MPa and 0.29 MPa, more preferably between 0.12 MPa and 0.28 MPa, even more preferably 0.13 MPa and 0.27 MPa. Such water stream 24 is a low-pressurized water stream.

[0181] For example, in that case wherein one or more solid oxide electrolyser cells 400 working in coelectrolysis mode (co-SOEC) are implied, the first additional stream of steam 25 can be at a pressure ranging between 0.1 1 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0182] For example, in that case wherein one or more solid oxide electrolyser cells 400 working in coelectrolysis mode (co-SOEC) are implied, the first additional stream of steam 25 can be at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0183] With preference, the step of pressure increase comprises increasing the pressure of the second part 29 of said first additional stream of steam into the range comprised between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa. In the installation represented at figure 5a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the thermal energy of the oxygen outflow 21 generated from the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) is transferred to a water stream 23, the process of methanol production is consuming at most 10.75 kWh / kgMeoH, preferably at most 10.70 kWh / kgMeoH

[0184] In the installation represented at figure 5b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the thermal energy of the oxygen outflow 21 generated from the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) is transferred to a water stream 23, the process of methanol production is consuming at most 10.00 kWh / kgMeoH, preferably at most 9.95 kWh / kgMeoH.

[0185] Further improvement by implying the thermal energy of the hydrogen-rich effluent from the one or more solid oxide electrolyser cells

[0186] More preferably, in either the first (figure 6a) or the second (figure 6b) embodiment, the method further comprises a step of transferring the thermal energy of respectively the hydrogen-rich effluent 15 or the syngas effluent 19 to the water stream 24 which is for example provided at a pressure below 0.32 MPa, before the step of transferring the thermal energy of the oxygen outflow 21 to said water stream 24 so as to generate the first additional stream of steam 25. For example, the installation further comprises a third heat exchanger placed on the water line upstream of the second heat exchanger, and the hydrogen-output line of each of said one or more solid oxide electrolyser cells 400 is connected to said third heat exchanger so that the thermal energy of the hydrogen-rich effluent 15 or the syngas effluent 19 is transferred to the water stream 24 directed into the water line upstream of the second heat exchanger.

[0187] For example, the water stream 24 can be at a pressure below 0.32 MPa, or below 0.30 MPa, preferably below 0.29 MPa, more preferably below 0.28 MPa, even more preferably below 0.27 MPa. For example, the water stream 24 can be at a pressure ranging between 0.10 MPa and 0.30 MPa, preferably between 0.1 1 MPa and 0.29 MPa, more preferably between 0.12 MPa and 0.28 MPa, even more preferably 0.13 MPa and 0.27 MPa. Such water stream 24 is a low-pressurized water stream.

[0188] It is noted the step of transferring the thermal energy of the first additional stream of steam 25 to the temperature-regulating device 250 of the separation unit is carried out on a first part 27 of said first additional stream of steam, and a second part 29 of said first additional stream of steam is subjected to a step of pressure increase, for example by directing said second part 29 of the first additional stream of steam into a second compressor 600 before being fed to said one or more solid oxide electrolyser cells 400. Indeed, the transfer of the thermal energy of the oxygen outflow 21 to the water stream 23 generate a first additional stream of steam 25 at pressure of at most 0.32 MPa, which provides an excess of the steam, namely the second part 29 of the first additional stream of steam that can thus be reused to feed the one or more solid oxide electrolyser cells 400.

[0189] For example, the first additional stream of steam 25 can be at a pressure ranging between 0.1 1 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0190] For example, the first additional stream of steam 25 can be at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0191] With preference, the step of pressure increase comprises increasing the pressure of the second part 29 of said first additional stream of steam into the range comprised between 0.35 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa.

[0192] In the installation represented at figure 6a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the thermal energy of the hydrogen-rich effluent 15 is transferred to a water stream 24 which is for example provided at a pressure below 0.32 MPa before that the thermal energy of the oxygen outflow 21 is transferred to it, the process of methanol production is consuming at most 10.65 kWh / kgMeoH, preferably at most 10.60 kWh / kgMeoH.

[0193] In the installation represented at figure 6b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the thermal energy of the syngas effluent 19 is transferred to a water stream 24 which is for example provided at a pressure below 0.32 MPa before that the thermal energy of the oxygen outflow 21 is transferred to it, the process of methanol production is consuming at most 9.85 kWh / kgMeoH, preferably at most 9.80 kWh / kgMeoH.

[0194] Improvement by steam production for feeding the one or more solid oxide electrolyser cells thanks to their own oxygen-containing effluent

[0195] With preference, and as represented at figures 7a and 7b, the installation further comprises a water supply upstream of a fourth heat exchanger, and a water line directing a water stream 23, which is for example at a pressure ranging between 0.32 MPa and 1.29 MPa, from said water supply to said fourth heat exchanger, wherein the installation further comprises a fourth line connecting the first heat exchanger with the fourth heat exchanger to direct an oxygen outflow 21 from said first heat exchanger to said fourth heat exchanger, so that the thermal energy of the oxygen outflow 21 is transferred to the water stream 23 directed into the water line to produce a second additional steam 31 of steam that is directed into an additional line connecting the fourth heat exchanger to the one or more solid oxide electrolyser cells 400. The thermal energy of the oxygen-containing effluent is therefore used to produce steam that is going to be reused for running the one or more solid oxide electrolyser cells 400.

[0196] For example, the water stream 23 can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa. Such water stream 23 is a medium-pressurized water stream.

[0197] Thus, the step of transferring the thermal energy of the oxygen-containing effluent 13 to the first stream 3 recovered in step (c) generates an oxygen outflow 21 ; and the method can further comprise the step of providing a water stream 23 and the step of transferring the thermal energy of at least the oxygen outflow 21 to said water stream 23 so as to generate a second additional stream 31 of steam, the method further comprises the step of feeding said second additional stream 31 of steam to said one or more solid oxide electrolyser cells 400.

[0198] For example, the second additional stream of steam 31 is at a pressure ranging between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa. For example, the second additional stream of steam 31 is at a temperature ranging between 142°C and 184°C, preferably between 143°C and 180°C, more preferably between 144°C and 175°C.

[0199] In the installation represented at figure 7a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the configuration allows its own steam production for running the one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC), the process of methanol production is consuming at most 10.75 kWh / kgMeoH, preferably at most 10.70 kWh / kgMeoH.

[0200] In the installation represented at figure 7b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the configuration allows its own steam production for running the one or more solid oxide electrolyser cells 400 working in co- electrolysis mode (co-SOEC), the process of methanol production is consuming at most 10.00 kWh / kgMeoH, preferably at most 9.95 kWh / kgMeoH.

[0201] Improvement by steam production for feeding the one or more solid oxide electrolyser cells thanks to both their own oxygen-containing effluent and their own hydrogen-rich effluent

[0202] For example, the installation further comprises a fifth heat exchanger placed on the water line upstream of the fourth heat exchanger, and the hydrogen-output line of each of said one or more solid oxide electrolyser cells 400 is connected to said fifth heat exchanger so that the thermal energy of the hydrogen-rich effluent 15 or the syngas effluent 19 is transferred to the water stream 23, which is for example at a pressure ranging between 0.32 MPa and 1 .29 MPa, directed into the water line upstream of the fourth heat exchanger.

[0203] For example, the water stream 23 can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa. Such water stream 23 is a medium-pressurized water stream.

[0204] Thus, in either the first or the second embodiment, the method can further comprise a step of transferring the thermal energy of respectively the hydrogen-rich effluent 15 or the syngas effluent 19 to the water stream 23 before the step of transferring the thermal energy of the oxygen outflow 21 to said water stream 23 so as to generate the second additional stream 31 of steam. This is implemented in the installation represented at figures 8a and 8b. In this implementation, the thermal energy of both the hydrogen-rich effluent 15 or the syngas effluent 19 and the oxygen-containing effluent 13 is used to produce steam that is going to be reused for running the one or more solid oxide electrolyser cells 400.

[0205] In the installation represented at figure 8a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the configuration allows its own steam production, thanks to both the hydrogen-rich effluent 15 and the oxygen-containing effluent 13, for running the one or more solid oxide electrolyser cells 400, the process of methanol production is consuming at most 10.70 kWh / kgMeoH, preferably at most 10.65 kWh / kgMeoH.

[0206] In the installation represented at figure 8b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when the configuration allows its own steam production, thanks to both the syngas effluent 19 and the oxygen-containing effluent 13, for running the one or more solid oxide electrolyser cells 400, the process of methanol production is consuming at most 9.95 kWh / kgMeoH, preferably at most 9.90 kWh / kgMeoH.

[0207] Improvement by steam production for improving the efficacy of the separation unit thanks to the one or more solid oxide electrolyser cells and their oxygen-containing effluent

[0208] Advantageously, the installation further comprises a water supply upstream of a sixth heat exchanger, and a water line directing a water stream 24, which is for example at a pressure below 0.32 MPa, from said water supply to said sixth heat exchanger; the installation further comprises one or more solid oxide electrolyser cells 400, each of said one or more solid oxide electrolyser cells 400 comprising an oxygen-output line to direct an oxygen-containing effluent 13 out of said solid oxide electrolyser cell 400; said oxygen-output line being in connection with the sixth heat exchanger so that the thermal energy of the said oxygen-containing effluent 13 is transferred to the water stream 24 directed into the water line, so as to produce a third additional stream 33 of steam that is directed into an additional line connecting the sixth heat exchanger to the temperature-regulating device 250.

[0209] For example, the water stream 24 can be at a pressure below 0.32 MPa, or below 0.30 MPa, preferably below 0.29 MPa, more preferably below 0.28 MPa, even more preferably below 0.27 MPa. For example, the water stream 24 can be at a pressure ranging between 0.10 MPa and 0.30 MPa, preferably between 0.1 1 MPa and 0.29 MPa, more preferably between 0.12 MPa and 0.28 MPa, even more preferably 0.13 MPa and 0.27 MPa. Such water stream 24 is a low-pressurized water stream.

[0210] Thus, the step of working said one or more solid oxide electrolyser cells 400 under electrical power further generates an oxygen-containing effluent 13; and the method can further comprise the step of providing a water stream 24, which is for example at a pressure below 0.32 MPa, and the step of transferring the thermal energy of at least the oxygen-containing effluent 13 to said water stream 23 so as to generate a third additional stream 33 of steam; and the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of the third additional stream 33 of steam to the temperatureregulating device 250 of the separation unit.

[0211] For example, the third additional stream of steam 33 is at a pressure ranging between 0.1 1 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa. For example, the third additional stream of steam 33 is at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C. This is implemented in the installation represented at figures 9a.

[0212] It is noted that in the case where the oxygen-containing effluent 13 is exiting the one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) (case of figure 9b), the step of transferring the thermal energy of the third additional stream of steam 33 to the temperature-regulating device of the separation unit is carried out on a first part 35 of said third additional stream of steam, and a second part 37 of said third additional stream of steam is subjected to a step of pressure increase, for example by directing said second part 37 of the third additional stream of steam into a second compressor 600 before being fed to said one or more solid oxide electrolyser cells 400. Indeed, the transfer of the thermal energy of the oxygen-containing effluent 13 to the water stream 23 generates a third additional stream of steam 33 at pressure of at most 0.32 MPa, which provides an excess of the steam, namely the second part 37 of the third additional stream of steam that can thus be reused to feed the one or more solid oxide electrolyser cells 400.

[0213] For example, in that case wherein one or more solid oxide electrolyser cells 400 working in coelectrolysis mode (co-SOEC) are implied, the third additional stream of steam 33 can be at a pressure ranging between 0.1 1 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0214] For example, in that case wherein one or more solid oxide electrolyser cells 400 working in coelectrolysis mode (co-SOEC) are implied, the third additional stream of steam 33 can be at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0215] With preference, the step of pressure increase comprises increasing the pressure of the second part 37 of said third additional stream of steam into the range comprised between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa.

[0216] In the installation represented at figure 9a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when steam is produced thanks to oxygencontaining effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) to run the temperature-regulating device of the separation unit, the process of methanol production is consuming at most 10.75 kWh / kgMeoH, preferably at most 10.70 kWh / kgMeOH. In the installation represented at figure 9b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when steam is produced thanks to oxygencontaining effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in coelectrolysis mode (co-SOEC) to run the temperature-regulating device of the separation unit, the process of methanol production is consuming at most 10.00 kWh / kgMeoH, preferably at most 9.95 kWh / kgMeoH.

[0217] Improvement by steam production for improving the efficacy of the separation unit thanks to the one or more solid oxide electrolyser cells and both its oxygen-containing effluent and its hydrogen-rich effluent

[0218] For example, as represented at figures 10a and 10b, the installation further comprises a seventh heat exchanger placed on the water line upstream of the sixth heat exchanger, and the hydrogen-output line of each of said one or more solid oxide electrolyser cells 400 is connected to said seventh heat exchanger so that the thermal energy of the hydrogen-rich effluent 15 or the syngas effluent 19 is transferred to the water stream 24 directed into the water line upstream of the sixth heat exchanger.

[0219] For example, the water stream 24 can be at a pressure below 0.32 MPa, or below 0.30 MPa, preferably below 0.29 MPa, more preferably below 0.28 MPa, even more preferably below 0.27 MPa. For example, the water stream 24 can be at a pressure ranging between 0.10 MPa and 0.30 MPa, preferably between 0.1 1 MPa and 0.29 MPa, more preferably between 0.12 MPa and 0.28 MPa, even more preferably 0.13 MPa and 0.27 MPa. Such water stream 24 is a low-pressurized water stream.

[0220] Thus, in either the first or the second embodiment, the method can further comprise a step of transferring the thermal energy of respectively the hydrogen-rich effluent 15 or the syngas effluent 19 to the water stream 24, which is for example at a pressure below 0.32 MPa, before the step of transferring the thermal energy of the oxygen-containing effluent 13 to said water stream 24 so as to generate the third additional stream of steam 33.

[0221] It is noted that the step of transferring the thermal energy of the third additional stream of steam 33 to the temperature-regulating device 250 of the separation unit is carried out on a first part 35 of said third additional stream of steam, and a second part 37 of said third additional stream of steam is subjected to a step of pressure increase, for example by directing said second part 37 of the third additional stream of steam into a second compressor 600 before being fed to said one or more solid oxide electrolyser cells 400. Indeed, the transfer of the thermal energy of the oxygen-containing effluent 13 to the water stream 24 generates a third additional stream of steam 33 at pressure of at most 0.32 MPa, which provides an excess of the steam, namely the second part 37 of the third additional stream of steam that can thus be reused to feed the one or more solid oxide electrolyser cells 400.

[0222] For example, the third additional stream of steam 33 can be at a pressure ranging between 0.1 1 MPa and 0.32 MPa, or between 0.12 MPa and 0.29 MPa, preferably between 0.13 MPa and 0.28 MPa, more preferably between 0.14 MPa and 0.27 MPa.

[0223] For example, the third additional stream of steam 33 can be at a temperature ranging between 102°C and 136°C, or between 105°C and 132°C, preferably between 107°C and 131 °C, more preferably between 109°C and 130°C.

[0224] With preference, the step of pressure increase comprises increasing the pressure of the second part 37 of said third additional stream of steam into the range comprised between 0.35 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa.

[0225] In the installation represented at figure 10a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when steam is produced thanks to both the hydrogen-rich effluent 15 and the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in electrolysis mode (SOEC) to run the temperatureregulating device of the separation unit, the process of methanol production is consuming at most 10.65 kWh / kgMeoH, preferably at most 10.60 kWh / kgMeoH.

[0226] In the installation represented at figure 10b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa and when steam is produced thanks to both the syngas effluent 19 and the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 working in co-electrolysis mode (co-SOEC) to run the temperatureregulating device of the separation unit, the process of methanol production is consuming at most 9.90 kWh / kgMeoH, preferably at most 9.85 kWh / kgMeoH.

[0227] Use of heat generated by one or more first compressors upstream of the reactor

[0228] As represented at figures 11a and 11 b, one or more first compressors 700 are placed upstream of the reactor 100 of the methanol-generating unit, namely upstream of the reactor inlet, so that the hydrogen-rich effluent 15 or the syngas effluent 19 exiting the one or more solid oxide electrolyser cells 400 is directed into said one or more first compressors 700 before being fed to the reactor 100. Under electrolysis mode (SOEC), a carbon oxides feedstock 16 is also directed into said one or more first compressors 700, before being fed to the reactor 100. The step of pressure increase of the hydrogen-rich effluent 15 or the syngas effluent 19 that is performed within said one or more first compressors 700 also generates heat. Then, a water stream 23 is provided, and there is a step of transferring the heat generated by said one or more first compressors 700 to said water stream 23, so that a fourth additional stream of steam 39 is generated and then fed to the one or more solid oxide electrolyser cells 400.

[0229] For example, the water stream 23 can be at a pressure ranging between 0.32 MPa and 1 .29 MPa, preferably between 0.32 MPa and 1.28 MPa, preferably between 0.32 MPa and 1.27 MPa, more preferably between 0.33 MPa and 1 .26 MPa, even more preferably between 0.34 MPa and 1 .25 MPa, most preferably between 0.35 MPa and 1 .24 MPa. Such water stream 23 is a medium-pressurized water stream.

[0230] With preference, the step of pressure increase of the hydrogen-rich effluent 15 comprises increasing the pressure to a range comprised between 0.32 MPa and 12.0 MPa, preferably between 0.5 MPa, and 9.5 MPa, more preferably between 1 .0 MPa and 9.0 MPa; even more preferably between 1.5 MPa and 8.5 MPa, most preferably between 2.0 MPa and 8.0 MPa. With preference, the step of pressure increase of the carbon oxides feedstock 16 comprises increasing the pressure at the same pressure as the pressure of the hydrogen-rich effluent 15, namely to a range comprised between 0.32 MPa and 12.0 MPa, preferably between 0.5 MPa, and 9.5 MPa, more preferably between 1 .0 MPa and 9.0 MPa; even more preferably between 1 .5 MPa and 8.5 MPa, most preferably between 2.0 MPa and 8.0 MPa.

[0231] In the case of co-electrolysis (co-SOEC), the step of pressure increase of the syngas effluent 19 comprises increasing the pressure to a range comprised between 0.32 MPa and 12.0 MPa, preferably between 0.5 MPa, and 9.5 MPa, more preferably between 1.0 MPa and 9.0 MPa; even more preferably between 1 .5 MPa and 8.5 MPa, most preferably between 2.0 MPa and 8.0 MPa.

[0232] For example, the fourth additional stream of steam 39 is at a pressure ranging between 0.38 MPa and 1.10 MPa, preferably between 0.39 MPa and 1.00 MPa, more preferably between 0.40 MPa and 0.90 MPa. For example, the fourth additional stream of steam 39 is at a temperature ranging between 142°C and 184°C, preferably between 143°C and 180°C, more preferably between 144°C and 175°C.

[0233] On these figures, a line connecting the reactor 100 to the separation unit, in particular to the distillation column 200, has been represented. This line conveys the reactor effluent 150 from the reactor 100 to the separation unit.

[0234] In the installation represented at figure 11a, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa, and when the one or more solid oxide electrolyser cells 400 are working in electrolysis mode (SOEC) are notably coupled to the reactor 100 of the methanol-generating unit via one or more first compressors 700, the process of methanol production is consuming at most 10.95 kWh / kgMeoH, preferably at most 10.90 kWh / kgMeoH.

[0235] In the installation represented at figure 11 b, namely when the second stream 5 exiting the turbine is at a pressure P2 of 0.25 MPa, and when the one or more solid oxide electrolyser cells 400 are working in co-electrolysis mode (co-SOEC) are notably coupled to the reactor 100 of the methanol-generating unit via one or more first compressors 700, the process of methanol production is consuming at most 10.30 kWh / kgMeoH, preferably at most 10.25 kWh / kgMeOH.

[0236] Examples

[0237] The advantages of the present disclosure are illustrated by the following examples. However, it is understood that the disclosure is no means limited to the specific examples.

[0238] Table 1 indicates the results of the simulation of the energy consumption in relation with the methanol production in accordance with the different heat management methods that have been described in case where a solid oxide electrolyser cell working into electrolysis mode (SOEC) is combined with the methanol-generating unit. The energy consumption which is saved (5) is given with respect to a method wherein only the second stream 5 exiting the turbine at a pressure P2 of 0.5 MPa is directed to the separation unit to transfer its thermal energy to the temperature-regulating device 250, in the case where the methanol-generating unit is combined with a solid oxide electrolyser cell working in electrolysis mode (SOEC) (figure 2a).

[0239] Table 1 : Results of simulation implying a heat management method comprising a solid oxide electrolyser cell working in electrolysis mode (SOEC) As indicated, one of the best configurations in term of energy consumption (j.e., figure 10a) is in the case where a step of transferring the thermal energy of the hydrogen-rich effluent 15 to a water stream 24 is carried out before transferring the thermal energy of the oxygencontaining effluent 13 to said water stream 24, so that the steam produced thanks to both the hydrogen-rich effluent 15 and the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 can be used to run the temperature-regulating device 250 of the separation unit.

[0240] As indicated, a second best configuration in term of energy consumption ( .e., figure 6a) is in the case where a step of transferring the thermal energy of the oxygen-containing effluent 13 to the first stream 3 recovered at step (c) so as to generate an oxygen outflow 21 followed by a step of providing a water stream 24. Then a step of transferring the thermal energy of the hydrogen-rich effluent 15 to the water stream 24 is carried out before a step of transferring the thermal energy of the oxygen outflow 21 , so as to generate a first additional stream 25. Finally, the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of a first part 27 of the first additional stream to the temperature-regulating device 250 of the separation unit. An excess of steam, namely a second part 29 of the first additional stream of steam is then fed, after a step of pressure increase from 0.25 MPa to 0.50 MPa, to the one or more electrolyser cells 400 working in electrolysis mode.

[0241] Table 2 indicates the results of the simulation of the energy consumption in relation with the methanol production in accordance with the different heat management methods that have been described in case where a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) is combined with the methanol-generating unit. The energy consumption which is saved (5) is given with respect to a method wherein only the second stream 5 exiting the turbine at a pressure P2 of 0.5 MPa is directed to the separation unit to transfer its thermal energy to the temperature-regulating device 250, in the case where the methanol-generating unit is combined with a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC) (figure 2b).

[0242] Table 2: Results of simulation implying a heat management method comprising a solid oxide electrolyser cell working in co-electrolysis mode (co-SOEC)

[0243]

[0244] As indicated, one of the best configurations in term of energy consumption (j.e., figure 6b) is in the case where a step of transferring the thermal energy of the oxygen-containing effluent 13 to the first stream 3 recovered at step (c) so as to generate an oxygen outflow 21 followed by a step of providing a water stream 24. Then a step of transferring the thermal energy of the syngas effluent 19 to the water stream 24 is carried out before a step of transferring the thermal energy of the oxygen outflow 21 , so as to generate a first additional stream 25. Finally, the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of a first part 27 of the first additional stream to the temperature-regulating device 250 of the separation unit. An excess of steam, namely a second part 29 of the first additional stream of steam is then fed, after a step of pressure increase from 0.25 MPa to 0.50 MPa, the one or more electrolyser cells 400 working in co-electrolysis mode.

[0245] As indicated, a second best configuration in term of energy consumption ( .e., figure 10b) is in the case where a step of transferring the thermal energy of the syngas effluent 19 to a water stream 24 is carried out before transferring the thermal energy of the oxygen-containing effluent 13 to said water stream 24, so that the steam produced thanks to both the hydrogenrich effluent 15 and the oxygen-containing effluent 13 exiting the one or more solid oxide electrolyser cells 400 can be used to run the temperature-regulating device 250 of the separation unit

Claims

Claims1. A heat management method in a methanol-generating unit, said method is characterized in that it comprises the following steps: a) providing a methanol-generating unit and a separation unit, wherein the separation unit is placed downstream of the methanol-generating unit and is in fluidic connection with it, wherein said separation unit comprises a temperature-regulating device (250), and wherein said methanol-generating unit comprises one or more reactors (100) each comprising a cooling device; b) operating said at least one reactor (100) under first operating conditions comprising at least regulating the thermal energy of said at least one reactor (100) by adjusting the temperature of the cooling device with water (1 ); c) recovering from said cooling device, after said step of regulating the thermal energy, a first stream (3), said first stream (3) comprising steam at a pressure P1 ; d) decreasing the pressure of said first stream (3) so as to recover a second stream (5), said second stream (5) comprising steam at a pressure P2, P2 being below 0.32 MPa and wherein P2 < P1 ; e) operating said separation unit under second operating conditions comprising regulating the thermal energy of said separation unit by transferring the thermal energy of at least the second stream (5) recovered at step (d) to the temperatureregulating device (250) of the separation unit.

2. The heat management method according to claim 1 , characterized in that the pressure P2 of the second stream (5) is ranging between 0.11 MPa and 0.32 MPa and / or in that the first stream (3) is at a temperature T1 comprised between 200°C and 325°C.

3. The heat management method according to claim 1 or 2, characterized in that the second stream (5) comprising steam at a pressure P2 further comprises one condensate; and in that the method further comprises the step of separating the steam from said one condensate so as to recover a third stream (7), said third stream (7) comprising steam at a pressure P3, wherein P3 is equal or inferior to P2; with preference, the step of regulating the thermal energy carried out in step (e) is the step of transferring the thermal energy of the third stream (7) to the temperature-regulating device (250) of the separation unit.

4. The heat management method according to any one of claims 1 to 3, characterized in that the method further comprises providing one or more solid oxide electrolyser cells (400), feeding said one or more solid oxide electrolyser cells (400) with steam (12), and working said one or more solid oxide electrolyser cells (400) under electrical power at a temperature higher than 400°C so as to generate at least a hydrogen-rich effluent (15); and in that the first operating conditions used at step (b) further comprises providing a carbon oxides feedstock to said at least one reactor, providing the hydrogen-rich effluent (15) generated by working said one or more solid oxide electrolyser cells (400) as a stream of hydrogen and mixing together the carbon oxides feedstock and the stream of hydrogen within said at least one reactor (100) so as to produce a methanol effluent; with preference, the method further comprises the step of increasing the pressure of said hydrogen containing-effluent (15) before using it as stream of hydrogen in the first operating conditions used at step (b).

5. The heat management method according to any one of claims 1 to 3, characterized in that the method further comprises providing one or more solid oxide electrolyser cells (400), feeding said one or more solid oxide electrolyser cells (400) with steam (12) and carbon dioxide (17), and working said one or more solid oxide electrolyser cells (400) under electrical power at a temperature higher than 400°C so as to generate at least a syngas effluent (19); and in that the first operating conditions used at step (b) further comprises providing the syngas effluent (19) generated by working said one or more solid oxide electrolyser cells (400) so as to produce a methanol effluent; with preference, the method further comprises the step of increasing the pressure of said syngas effluent (19) before using it as stream of hydrogen in the first operating conditions used at step (b) and / or the step of feeding said one or more solid oxide electrolyser cells (400) with steam (12) and carbon dioxide (17) further comprises feeding said one or more solid oxide electrolyser cells (400) with hydrogen, syngas, methane, hydrocarbons, or a mixture thereof.

6. The heat management method according to claim 4 or 5, characterized in that the step (b) of operating said at least one reactor (100) generates a reactor effluent (150), and wherein the method further comprises the step of providing a water stream (23) and the step of transferring the thermal energy of said reactor effluent (150) to said water stream (23) so as to generate a fifth additional stream of steam (41 ), said fifth additional stream of steam (41 ) being then fed to said one or more solid oxide electrolyser cells(400); with preference, said water stream (23) provided to generate the fifth additional stream of steam (41 ) is at a pressure ranging between 0.32 MPa and 1 .29 MPa.

7. The heat management method according to claim 4 to 6, characterized in that the step (d) of decreasing the pressure of said first stream (3) further produces electrical energy; and in that the method further comprises the step of supplying said electrical energy to said one or more solid oxide electrolyser cells (400) so as to run said one or more solid oxide electrolyser cells (400); and / or in that the methanol-generating unit provided at step (a) comprises one or more first compressors (700), and the step (d) of decreasing the pressure of said first stream (3) further produces electrical energy and / or shaft work; and the method further comprises the step of supplying said electrical energy and / or shaft work to said one or more first compressors (700) so as to run the one or more first compressors (700) comprised within the methanol-generating unit.

8. The heat management method according to any one of claims 4 to 7, characterized in that the step of working said one or more solid oxide electrolyser cells (400) under electrical power further generates an oxygen-containing effluent (13), and in that the method further comprises the step of transferring the thermal energy of the oxygencontaining effluent (13) to the first stream (3) recovered at step (c).

9. The heat management method according to claim 8, characterized in that the step of transferring the thermal energy of the oxygen-containing effluent (13) to the first stream (3) recovered in step (c) generates an oxygen outflow (21 ); and the method further comprises the step of providing a water stream (23) at a pressure ranging between between 0.32 MPa and 1 .29 MPa and the step of transferring the thermal energy of at least the oxygen outflow (21 ) to said water stream (23) so as to generate a first additional stream of steam (25), and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said first additional stream of steam (25) to the temperature-regulating device (250) of the separation unit.

10. The heat management method according to claim 8, characterized in that the step of transferring the thermal energy of the oxygen-containing effluent (13) to the first stream (3) recovered in step (c) generates an oxygen outflow (21 ); and the method furthercomprises the step of providing a water stream (24) at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygen outflow (21 ) to said water stream (24) so as to generate a first additional stream of steam (25), and wherein the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of said first additional stream of steam (25) to the temperature-regulating device (250) of the separation unit ; with preference, the method further comprises a step of transferring the thermal energy of either the hydrogen-rich effluent (15) or the syngas effluent (19) to the water stream (24) at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen outflow (21 ) to said water stream (24) so as to generate the first additional stream of steam (25).1 1 . The heat management method according to claim 10, characterized in that, the step of transferring the thermal energy of said first additional stream of steam (25) to the temperature-regulating device (250) of the separation unit is carried out on a first part (27) of said first additional stream of steam, and a second part (29) of said first additional stream of steam is subjected to a step of pressure increase before being fed to said one or more solid oxide electrolyser cells (400).

12. The heat management method according to claim 8, characterized in that the step of transferring the thermal energy of the oxygen-containing effluent (13) to the first stream (3) recovered in step (c) generates an oxygen outflow (21 ); and the method further comprises the step of providing a water stream (23) at a pressure ranging between 0.32 MPa and 1 .29 MPa and the step of transferring the thermal energy of at least the oxygen outflow (21 ) to said water stream (23) so as to generate a second additional stream of steam (31 ), the method further comprises the step of feeding said second additional stream of steam (31 ) to said one or more solid oxide electrolyser cells (400); with preference, the method further comprises a step of transferring the thermal energy of either the hydrogen-rich effluent (15) or the syngas effluent (19) to the water stream (23) at a pressure ranging between 0.32 MPa and 1.29 MPa before the step of transferring the thermal energy of the oxygen outflow (21 ) to said water stream (23) so as to generate the second additional stream of steam (31 ).

13. The heat management method according to any one of claims 4 to 8, characterized in that the step of working said one or more solid oxide electrolyser cells (400) under electrical power further generates an oxygen-containing effluent (13); in that the method further comprises the step of providing a water stream (24) at a pressure below 0.32 MPa and the step of transferring the thermal energy of at least the oxygencontaining effluent (13) to said water stream (24) so as to generate a third additional stream of steam (33); and in that the step of regulating the thermal energy carried out in step (e) further comprises transferring the thermal energy of the third additional stream of steam (33) to the temperature-regulating device (250) of the separation unit; with preference, the method further comprises a step of transferring the thermal energy of either the hydrogen-rich effluent (15) or the syngas effluent (19) to the water stream (24) at a pressure below 0.32 MPa before the step of transferring the thermal energy of the oxygen-containing effluent (13) to said water stream (24) so as to generate the third additional stream of steam (33).

14. The heat management method according to claim 13, characterized in that the step of transferring the thermal energy of said third additional stream of steam (33) to the temperature-regulating device (250) of the separation unit is carried out on a first part (35) of said third additional stream of steam, and a second part (37) of said third additional stream of steam is subjected to a step of pressure increase before being fed to said one or more solid oxide electrolyser cells (400).

15. The heat management method according to any one of claims 8 to 14, characterized in that the hydrogen-rich effluent (15) or the syngas effluent (19) is subjected to a pressure increase step before being directed to the reactor (100), said pressure increase step generating heat, and that the method further comprises the step of providing a water stream (23) and the step of transferring the heat generated by the pressure increase step to said water stream (23) so as to generate a fourth additional stream of steam (39), said fourth additional stream of steam (39) being then fed to said one or more solid oxide electrolyser cells (400); with preference, said water stream (23) provided to generate the fourth additional stream of steam (39) is at a pressure ranging between 0.32 MPa and 1 .29 MPa.

16. An installation for producing methanol, said installation is characterized in that it comprises:- a methanol-generating unit and a separation unit, wherein said separation unit is placed downstream of the methanol-generating unit and is in fluidic connection with it, wherein the separation unit comprises a temperature-regulating device (250), and wherein the methanol-generating unit comprising one or more reactors (100), each reactor (100) comprising a cooling device;- at least one steam pressure-reducing device, the steam pressure-reducing device being placed downstream of said cooling device and upstream of said temperatureregulating device (250);- a first line connecting fluidically the cooling device to the one or more steam pressurereducing devices;- a second line connecting fluidically the one or more steam pressure-reducing devices to the temperature-regulating device (250), and wherein the one or more steam pressure-reducing devices comprise at least one steam pressure regulator; with preference, the one or more steam pressure regulators are one or more pressure control valves; and / or one steam pressure-reducing device is at least one turbine (300).

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