Efficient use of heat in e-methanol plant

Abstract

A methanol plant and process for producing methanol are provided. A first SOE section is arranged to receive a carbon dioxide-rich feed and electrolyse it to a carbon monoxide-rich stream. A methanol loop is arranged to receive at least a portion of the carbon monoxide-rich stream and a hydrogen-rich stream and convert them to a crude methanol stream. A first H2O-rich stream is converted to a first steam stream by means of heat from the electrolysis process in the first SOE section. The first steam stream is used it as heat for the distillation of the crude methanol stream in the methanol distillation section.

Description

[0001] EFFICIENT USE OF HEAT IN E-METHANOL PLANT

[0002] TECHNICAL FIELD

[0003] The present invention relates to a methanol plant and process for producing methanol using said plant. A first SOE section is arranged to receive a carbon dioxide-rich feed and electrolyse it to a carbon monoxide-rich stream. A methanol loop is arranged to receive at least a portion of the carbon monoxide-rich stream and a hydrogen-rich stream and convert them to a crude methanol stream. A first H2O-rich stream is converted to a first steam stream by means of heat from the electrolysis process in the first SOE section. The first steam stream is used it as heat for the distillation of the crude methanol stream in the methanol distillation section.

[0004] BACKGROUND

[0005] Consistent efforts are being made to replace fossil fuels and to move towards sustainable production and storage of energy and chemicals. An important contribution to drive such efforts is "Power-to-X" (PtX), which relates to systems and methods enabling electricity conversion, energy storage, and reconversion pathways to use electric power from wind and solar power generation to store energy in the form of chemicals such as synthetic alcohols, synthetic fuels or substitute natural gas.

[0006] One way to use electric power is to electrolyse water to produce H2. It is known then to combine the H2and a CO2into a mixed stream, and convert the mixed stream to a CO- and H2-rich synthesis gas, which can be further converted to valuable products like alcohols (including methanol). However, at present, it is often ineffective and energy consuming to produce synthesis gas for synthetic alcohols from H2and CO2.

[0007] Recent developments have disclosed e-methanol plants which combining a H2-rich stream from H2O electrolysis with a CO-rich stream from CO2electrolysis to provide a syngas stream, which is then used in methanol synthesis.

[0008] However, there is a general need for further development of such plants to make them feasible for sustainable production and bring energy consumption down, hereby lowering the CO2footprint of such systems and methods. One particular goal is to make effective use of heat generated in one section of the plant in other sections. SUMMARY

[0009] It has been found by the present inventor(s) that heat generated by an electrolysis process can advantageously be used in methanol distillation.

[0010] A methanol plant is therefore provided, said methanol plant comprising : a carbon dioxide-rich feed; a first H2O-rich stream; a first solid oxide electrolysis (SOE) section; a second electrolysis section; a methanol loop; a methanol distillation section; wherein the first SOE section is arranged to receive the carbon dioxide-rich feed and electrolyse it in a first electrolysis process and to output a carbon monoxide-rich stream and an oxygen enriched stream (12); wherein the second electrolysis section is arranged to output a hydrogen-rich stream; wherein said methanol loop is arranged to receive at least a portion of the carbon monoxide-rich stream and at least a portion of the hydrogen-rich stream and convert them to a crude methanol stream; wherein said methanol distillation section is arranged to receive the crude methanol stream from the methanol loop and distil it, to thereby output a purified methanol product stream; wherein the methanol plant is further arranged to receive the first H2O-rich stream and convert it to a first steam stream by means of heat from the electrolysis process in the first SOE section; and wherein said methanol distillation section is arranged to receive said first steam stream and use it as heat for the distillation of the crude methanol stream.

[0011] A process is also provided for producing methanol, in the plant as described herein, said process comprising the steps of: feeding a carbon dioxide-rich feed to a first SOE section and electrolysing it in a first electrolysis process to a carbon monoxide-rich stream and an oxygen-enriched stream; outputting a hydrogen-rich stream from a second electrolysis section; feeding at least a portion of the carbon monoxide-rich stream and at least a portion of the hydrogen-rich stream to a methanol loop and converting them to a crude methanol stream; feeding the crude methanol stream from the methanol loop to the methanol distillation section and distilling it, to thereby output a purified methanol product stream; converting a first H2O-rich stream to a first steam stream by transferring heat from the first electrolysis process in the first SOE section; feeding said first steam stream to the methanol distillation section and using it as heat for the distillation of the crude methanol stream.

[0012] Further details of the system and process for producing the synthesis gas stream, and the related plants, are specified in the following detailed description, figures and claims.

[0013] LEGENDS

[0014] Fig. 1 shows a schematic overview of a methanol plant according to a first aspect.

[0015] Fig. 2 shows a more detailed schematic overview of the methanol plant of figure 1.

[0016] DETAILED DISCLOSURE

[0017] Unless otherwise specified, any given percentages for gas content are % by volume. The terms "synthesis gas" and "syngas" are used interchangeably in this text.

[0018] A methanol plant is provided. The methanol plant comprises: a carbon dioxide-rich feed; a first H2O-rich stream; a first solid oxide electrolysis (SOE) section; a second electrolysis section; a methanol loop; and a methanol distillation section. Overall, a conversion of CO2to methanol takes place in the plant.

[0019] First SOE section

[0020] The first solid oxide electrolysis SOE section is arranged to receive the carbon dioxide-rich feed and electrolyse it to a carbon monoxide-rich stream.

[0021] The carbon dioxide-rich feed is specified as being rich in carbon dioxide such as comprising more than 97 vol.% carbon dioxide, preferably more than 98 vol.% or more than 99%. Carbon dioxide-rich stream comprises carbon dioxide from external sources such as from biogas upgrading or fossil fuel-based syngas (synthesis gas) plants or biomass and / or fossil fuel based powerplant or from cement production or from fermentation processes like ethanol production.

[0022] The first solid oxide electrolysis (SOE) section comprises a solid oxide electrolysis cell (SOEC) such as one or more SOECs arranged in an SOEC stack. The solid oxide electrolysis cell is a solid oxide fuel cell (SOFC) run in reverse mode, which uses a solid oxide or ceramic electrolyte to produce a carbon monoxide-rich stream.

[0023] Specifically for the first SOE section, CO2is led to the fuel side of the cell with an applied current and excess oxygen is transported to the oxygen side of the cell (e.g. anode side), so as to electrolyse CO2to CO. Thus, the first SOE section provides a carbon monoxide-rich stream from the fuel side of the cell and a first oxygen-enriched stream from the oxygen side of the cell. The carbon monoxide-rich stream provided by the first SOE section comprises a mixture of CO and CO2, wherein the content of CO is preferably 20-80%.

[0024] Optionally, a flushing gas stream such as air or nitrogen is led to the oxygen side to flush the oxygen side. Flushing the oxygen side of the SOE has two advantages, i) reducing the oxygen concentration and related corrosive effects within the cell and ii) providing means for feeding energy into the first SOE as the operation is endothermic.

[0025] In embodiments, the carbon monoxide-rich stream comprising a mixture of CO and CO2, is arranged to be led to a separation unit such as to a pressure swing adsorption (PSA) unit, temperature swing adsorption (TSA) membrane separation unit, cryogenic separation unit, or liquid scrubber technology unit, such as a wash with N-methyl-diethyanolamine (MDEA). The purpose of the separation unit is to produce a further enriched carbon monoxide-rich stream and a balance stream enriched in carbon dioxide. In embodiments, the balance stream may be either recycled to the carbon monoxide-rich stream arranged to be fed to one or more separation units and / or to the inlet of the first SOE section for further conversion, optionally admixed with the carbon dioxide-rich feed. In this way, the exact composition of the carbon monoxide-rich stream may vary. In all embodiments the carbon monoxide-rich stream may be a further enriched carbon monoxide stream.

[0026] In alternative preferred embodiments, the electrolysis of CO2is conducted as a once-through operation, i.e. the SOE section is a once-through electrolysis unit. The term "once-through" means that there is no need for recycling of CO2. Compared to traditional systems for conducting CO2electrolysis, this enables that the need for a recycle compressor is eliminated, and thereby also the need for valves, pipes, and control system. Attendant operating expenses such as electric power needed for the compressor as well as maintenance of the recycle compressor and the other equipment (such as valves and pipes), are thereby saved. Moreover, the need for a pressure swing adsorption (PSA) unit is also eliminated, thereby significantly simplifying the system, process and plant for producing the synthesis gas for further conversion. Additionally, the once-through SOE section for CO2electrolysis may be operated with partial conversion, hereby mitigating the risk of carbon formation within the SOE section. In alternative embodiments, a portion of the carbon monoxide rich stream may be recycled to the inlet of the first SOE section for further conversion, optionally admixed with the carbon dioxide-rich feed.

[0027] In embodiments, the system further comprises one or more heating unit(s) arranged to heat the carbon dioxide-rich feed and / or optionally the flush gas stream. Preferably, the operation temperature of the one or more heating unit(s) is at least the operation temperature of the first SOE section plus 50°C, preferably at least the operation temperature of the first SOE section. In this way, heat may be supplied to the SOE section.

[0028] In preferred embodiments, the first solid oxide electrolysis (SOE) section operates in the temperature range of 500-900 °C, preferably 700-800 °C. Operating at these temperatures provides advantages of higher conversion efficiencies than low-temperature electrolysis because of favourable thermodynamics and kinetics at higher operating temperatures. In addition, high temperature operation results in lower operation expenses due to lower cell voltage as well as lower capital expenses to higher current densities.

[0029] Independent of embodiments, the first SOE section is arranged to receive the carbon dioxiderich feed and provide a carbon monoxide-rich stream and preferably a first oxygen enriched stream. First H2O-rich stream and heat exchange

[0030] The first H2O-rich stream may be water-rich, such as comprising more than 90% water, preferably 99% water. Additionally, or alternatively, the H2O-rich stream may comprise a first portion of steam. Preferably, the H2O-rich stream has a high purity, such as 99 vol% H2O. In embodiment, the first H2O-rich stream may be provided from a water treatment unit. The first H2O-rich stream may be exemplified by the following composition:

[0031] DMW purity(quality) pH value at 25°C pH 6-7,

[0032] Specific conductivity at 25°C (pS / cm) < 0.2,

[0033] Iron, total (Fe) (mg / kg) < 0.02,

[0034] Copper, total (Cu) (mg / kg) < 0.003,

[0035] Sodium (Na) (mg / kg) < 0.01,

[0036] KMnO4 consumpt.,

[0037] Mn(VII)— Mn(II), as KMnO4 (mg / kg) < 3,

[0038] Oil, grease (mg / kg) < 1.

[0039] The first H2O-rich stream may have a temperature of between 0 to 200 °C, preferably the first H2O-rich is a water-rich stream and with a temperature between 30 and 130 °C. The pressure of the first H2O-rich stream may be 1-20 bar g preferably 2-5 bar g.

[0040] The methanol plant is further arranged to receive the first H2O-rich stream and convert it to a first steam stream by means of heat from the electrolysis process in the first SOE section.

[0041] Conversion of the first H2O-rich stream to the first steam stream may take place via direct or indirect heating. In the present context direct heating is meant to refer to a transfer of heat from the heat source directly through a heat transfer wall to the stream to be heated and indirect heating is meant to refer to a transfer of heat from the heat source via an intermediate heat transfer medium, the heat transfer medium transferring the heat through a heat transfer wall to the stream to be heated.

[0042] In one aspect, the methanol plant further comprises a heat exchanger section comprising one or more heat exchangers. In an embodiment the heat exchanger section comprises a first and a second heat exchanger. The first and second heat exchangers may be independently selected from double pipe heat exchanger, shell-and-tube heat exchanger, plate heat exchanger or cross flow exchanger. Preferably, in embodiments, said first and said second heat exchangers are shell-and-tube heat exchangers. The first and second heat exchangers may be cross flow exchangers. The flow of streams within the heat exchangers may be arranged as parallel-flow, counterflow or cross-flow flow arrangement. In preferred embodiments, the flow of streams is arranged as counter-flow of streams. Counter-flow of streams is advantageous in embodiments, wherein the heat transfer results primarily in an increase in temperature such as providing a heated or evaporated H2O-rich stream. The counter-flow of streams allows for optimised heat transfer efficiency (heat transfer per unit mass) because the average temperature difference along any unit length is higher compared to alternative flow arrangements. In more preferred embodiments, the flow of streams is arranged as cross-flow of streams. Cross flow of streams is particularly advantageous in embodiments wherein the heat transfer results primarily in a phase transition such as a transition from water to steam.

[0043] In embodiments, where both of i) at least a portion of the carbon monoxide-rich stream and ii) at least a portion of the first oxygen enriched stream are arranged to transfer heat, it is preferred that said portions i) and ii) are arranged with the same flow arrangement.

[0044] In one aspect, the said heat exchanger section may be arranged to receive the carbon monoxide-rich stream and the first H2O-rich stream and to transfer heat from the carbon monoxide-rich stream to the first H2O-rich stream and to output the first steam stream and a cooled carbon monoxide-rich stream.

[0045] The heat exchanger section may further be arranged to transfer heat from the first oxygen enriched stream to the first H2O-rich stream and to further output a cooled first oxygen enriched stream. In this manner, heat transfer to the first H2O-rich stream can be optimised by selecting to transfer heat from the carbon monoxide-rich stream and / or the first oxygen enriched stream.

[0046] Allowing thermal communication between at least a portion of the carbon monoxide-rich stream and at least a portion of the first H2O-rich feed has the advantage of further cooling the carbon monoxide-rich stream, which is desirable when forming the synthesis gas from the cooled carbon monoxide-rich stream. In this way, providing a cooled carbon monoxiderich stream may eliminate or reduce the need of separate cooling systems or allow the capacity of such cooling systems to be reduced.

[0047] Suitably, the first H2O-rich stream is external to the plant (i.e. a feed to the plant).

[0048] Alternatively, or additionally, the first H2O-rich stream is at least a portion of an off-gas stream from the methanol loop and / or the methanol distillation section. The heat exchanger section of the methanol plant according to the invention may further comprise a steam drum arranged to vaporize liquid water to steam by means of heat from at least one of the carbon monoxide-rich stream and the first oxygen enriched stream.

[0049] Second electrolysis section

[0050] The second electrolysis section is arranged to output a hydrogen-rich stream.

[0051] In one aspect, the second electrolysis section is a second solid oxide electrolysis (SOE) section. According to this aspect, the methanol plant further comprises a second H2O-rich stream, wherein said second solid oxide electrolysis (SOE) section is arranged to receive at least a portion of the second H2O-rich stream, and electrolyse it to said hydrogen-rich stream.

[0052] The second electrolysis section may also be arranged to provide a second oxygen-enriched stream.

[0053] The second SOE section uses solid oxide or ceramic electrolyte to produce the hydrogen-rich stream. More specifically, the second H2O-rich stream is led to the fuel side of the cell with an applied current and excess oxygen is transported to the oxygen side of the cell (e.g. anode side), such to electrolyse H2O to hydrogen. Optionally, a flushing gas stream such as air or nitrogen is led to the oxygen side to flush the oxygen side. This leads to the second SOE section providing a hydrogen-rich stream from the fuel side of the cell and a second oxygen- enriched stream from the oxygen side of the cell. The hydrogen-rich stream provided by the second electrolysis section suitably comprises H2and steam, wherein the content of H2is between 20-100%, preferably 40-80%.

[0054] In embodiments, the system further comprises an external second H2O-rich stream (i.e. a second H2O-rich feed) which may be in the form of a second steam stream, being arranged to be fed to the second solid oxide electrolysis (SOE) section. The external second steam stream may be provided from a water treatment system such being of high purity such as 99.99% H2O. The external second steam stream may have a temperature of 100-210 °C, preferably 130-160 °C and a pressure of 1-19 bar g, preferably 1-4 bar g at the inlet of the SOE.

[0055] In embodiments, the system further comprises one or more heating unit(s) arranged to heat the external second steam stream and / or optionally the flush gas stream. Preferably, the operation temperature of the one or more heating unit(s) is / are at least the operation temperature of the second electrolysis section plus 50 °C, preferably at least the operation temperature of the second electrolysis section. In this way, heat may be supplied to the second electrolysis section.

[0056] In preferred embodiments, when the second electrolysis section is a second solid oxide electrolysis (SOE) section, it operates in the temperature range of 500-900 °C, preferably 700-800 °C. In embodiments, the system further comprises one or more heating unit(s) arranged to provide additional heat to the second SOE section during operation. The one or more heating unit(s) may comprise feed effluent exchangers and / or electrical heaters.

[0057] Methanol loop

[0058] A methanol loop (also called a methanol synthesis section) is arranged to receive at least a portion of the carbon monoxide-rich stream and at least a portion of the hydrogen-rich stream and convert them to a crude methanol stream. An off-gas stream is also produced.

[0059] The methanol synthesis reactor in the methanol loop accommodates the following two reactions:

[0060] CO2+ H2< = > CO + H2O

[0061] CO + 2H2< = > CH3OH

[0062] The process can occur, for example by sending the combined streams through a boiling water reactor, where at least a portion of the combined streams gas is converted to methanol followed by condensation and separation of the methanol in liquid phase, where the methanol in liquid phase therefrom is comprised in the methanol stream. Off-gas stream is produced in this process. The off-gas stream from the methanol synthesis section typically comprises: 85- 90% H2, 5-10% CO2, 0-3% CO.

[0063] The crude methanol product stream comprises a major portion of methanol, e.g. 60-65% methanol and 35-40% H2O by weight. Other minor components of this stream include but not limited to, higher alcohols, ketones, aldehydes, dimethyl ether (DME), organic acids and dissolved gases.

[0064] To obtain an optimized yield in the methanol production, the stoichiometry of H2, CO and CO2needs to be considered. In a preferred embodiment, the stoichiometry of H2, CO and CO2in the combined stream (syngas stream) falls within an interval such that the combined stream has a module between 1.8 and 2.2, preferably between 1.9 and 2.1, where the module is defined in terms of molar content: M = (H2-CO2) / (CO+CO2).

[0065] The module of the syngas stream may be adjusted by addition of a (further) hydrogen-rich stream, which is optionally arranged to be admixed with the syngas stream. The hydrogenrich stream can be provided by an external feed of hydrogen.

[0066] Methanol distillation section

[0067] Methanol distillation section is arranged to receive the crude methanol stream from the methanol loop and distil it, to thereby output a purified methanol product stream.

[0068] The distillation section is arranged to upgrade the crude methanol stream to a purified methanol product stream of the required grade, e.g. >95%, >98% or >99% methanol.

[0069] The methanol distillation section is arranged to receive said first steam stream and use it as heat for the distillation of the crude methanol stream. In this manner, effective use of heat from elsewhere in the plant is ensured.

[0070] Process

[0071] A process for producing methanol in the plant as described herein is also provided. This process comprising the steps of: feeding the carbon dioxide-rich feed to the first SOE section and electrolysing it to a carbon monoxide-rich stream; outputting a hydrogen-rich stream from the second electrolysis section; feeding at least a portion of the carbon monoxide-rich stream and at least a portion of the hydrogen-rich stream to the methanol loop and converting them to a crude methanol stream; feeding the crude methanol stream from the methanol loop to the methanol distillation section and distilling it, to thereby output a purified methanol product stream; converting the first H2O-rich stream to a first steam stream by means of heat from the electrolysis process in the first SOE section; feeding said first steam stream to the methanol distillation section and using it as heat for the distillation of the crude methanol stream. The process according to the invention the transfer of heat from the first electrolysis process may be achieved by transferring heat from i) at least a portion of the carbon monoxide-rich stream (11) and / or ii) at least a portion of the first oxygen enriched stream (12).

[0072] Suitably, the temperature of at least one of i) at least a portion of the carbon monoxide-rich stream and / or ii) at least a portion of the first oxygen enriched stream is / are in the range of 500-200 °C and the pressure of at least one of i) at least a portion of the carbon monoxiderich stream and / or ii) at least a portion of the first oxygen enriched stream is / are in the range of 0 -3 bar g.

[0073] In one aspect, the first solid oxide electrolysis (SOE) section operates in the temperature range of 500-900 °C, preferably 700-800 °C. The second electrolysis section may be a solid oxide electrolysis (SOE) section operating in the temperature range of 500-900 °C, preferably 700-800 °C. The temperature of the first steam stream is suitably between 100 - 210 °C, preferably 150 - 180 °C and the pressure of the first steam stream (13) is between 3.5 - 9 bar g.

[0074] Specific embodiments

[0075] Figure 1 shows a methanol plant (100) comprising the following components: carbon dioxide-rich feed (1); first H2O-rich stream (2); first solid oxide electrolysis (SOE) section (10); second electrolysis section (20); methanol loop (30); methanol distillation section (40).

[0076] The first SOE section (10) receives the carbon dioxide-rich feed (1) and electrolyses it to a carbon monoxide-rich stream (11). The second electrolysis section (20) outputs a hydrogenrich stream (21). The methanol loop (30) receives at least a portion of the carbon monoxiderich stream (11) and at least a portion of the hydrogen-rich stream (21) and convert them to a crude methanol stream (31). Methanol distillation section (40) receives the crude methanol stream (31) from the methanol loop (30) and distils it, to thereby output a purified methanol product stream (41). The first H2O-rich stream (2) is converted to a first steam stream (13) by means of heat from the electrolysis process in the first SOE section (10). The methanol distillation section (40) receives the first steam stream (13) and uses it as heat for the distillation of the crude methanol stream (31). In the more developed embodiment of Figure 2, the methanol plant further comprises a heat exchanger section (50). The first SOE section (10) receives the carbon dioxide-rich feed (1) and electrolyses it to a carbon monoxide-rich stream (11) and a first oxygen enriched stream (12). The heat exchanger section (50) transfers heat from the first oxygen enriched stream (12) to the first H2O-rich stream (2). A first steam stream (13), a cooled carbon monoxiderich stream (11') and a cooled first oxygen enriched stream (12') are outputted from the heat exchanger section (50). In Figure 2, the cooled carbon monoxide-rich stream (11') and at least a portion of the hydrogen-rich stream (21) are fed to the methanol loop (30) and converted to a crude methanol stream (31), which is then used as per Figure 1. EXAMPLE

[0077] In the following, the use of the invention is exemplified. The external heat required to be input to the distillation section of a 300 MTPD methanol plant based on CO2and hydrogen and feedstock can be reduced. From the table it can be seen that the steam generated in the CO2electrolysis section covers 7.5% of the total required steam for obtaining a grade AA methanol product in the distillation.

Claims

CLAIMS1. A methanol plant (100), said methanol plant comprising: a carbon dioxide-rich feed (1); a first H2O-rich stream (2); a first solid oxide electrolysis (SOE) section (10); a second electrolysis section (20); a methanol loop (30); a methanol distillation section (40); wherein the first SOE section (10) is arranged to receive the carbon dioxide-rich feed (1) and electrolyse it in a first electrolysis process and to output a carbon monoxide-rich stream (11) and an oxygen-enriched stream (12); wherein the second electrolysis section (20) is arranged to output a hydrogen-rich stream (21); wherein said methanol loop (30) is arranged to receive at least a portion of the carbon monoxide-rich stream (11, 11') and at least a portion of the hydrogen-rich stream (21) and convert them to a crude methanol stream (31); wherein said methanol distillation section (40) is arranged to receive the crude methanol stream (31) from the methanol loop (30) and distil it, to thereby output a purified methanol product stream (41); wherein the methanol plant (100) is further arranged to receive the first H2O-rich stream (2) and convert it to a first steam stream (13) by means of heat from the first electrolysis process in the first SOE section (10); and wherein said methanol distillation section (40) is arranged to receive said first steam stream (13) and use it as heat for the distillation of the crude methanol stream (31).

2. The methanol plant (100) according to claim 1, further comprising a heat exchanger section (50), said heat exchanger section (50) being arranged to receive the carbon monoxide-rich stream (11) and the first H2O-rich stream (2) and to transfer heat from the carbon monoxide-rich stream (11) to the first H2O-rich stream (2) and to output the first steam stream (13) and a cooled carbon monoxide-rich stream (11').

3. The methanol plant (100) according to any one of the preceding claims, wherein the second electrolysis section (20) is a second solid oxide electrolysis (SOE) section, said methanol plant (100) further comprising a second H2O-rich stream (3), wherein said second solid oxide electrolysis (SOE) section is arranged to receive at least a portion of the second H2O-rich stream (3), and electrolyse it to said hydrogen-rich stream (21).

4. The methanol plant (100) according to any one of claims 2-3, wherein said heat exchanger section (50) is further arranged to transfer heat from the first oxygen enriched stream (12) to the first H2O-rich stream (2) and to output a cooled first oxygen enriched stream (12').

5. The methanol plant (100) according to any one of the preceding claims, wherein the first H2O-rich stream (2) is external to the plant (i.e. a feed to the plant).

6. The methanol plant (100) according to any one of claims 1-4, wherein the first H2O- rich stream (2) is at least a portion of an off-gas stream from the methanol loop (30) and / or the methanol distillation section (40).

7. The methanol plant (100) according to any one of claims 2-6, wherein the heat exchanger section (50) comprises a steam drum arranged to vaporize liquid water to steam by means of heat from at least one of the carbon monoxide-rich stream (11) and the first oxygen enriched stream (12).

8. A process for producing methanol, said process comprising the steps of: feeding a carbon dioxide-rich feed (1) to a first SOE section (10) and electrolysing it in a first electrolysis process to a carbon monoxide-rich stream (11) and an oxygen- enriched stream (12); outputting a hydrogen-rich stream (21) from a second electrolysis section (20); feeding at least a portion of the carbon monoxide-rich stream (11, 11') and at least a portion of the hydrogen-rich stream (21) to a methanol loop (30) and converting them to a crude methanol stream (31); feeding the crude methanol stream (31) from the methanol loop (30) to the methanol distillation section (40) and distilling it, to thereby output a purified methanol product stream (41); converting a first H2O-rich stream (2) to a first steam stream (13) by transferring heat from the first electrolysis process in the first SOE section (10);feeding said first steam stream (13) to the methanol distillation section (40) and using it as heat for the distillation of the crude methanol stream (31).

9. The process according to claim 8, wherein the transfer of heat from the first electrolysis process is achieved by transferring heat from i) at least a portion of the carbon monoxide-rich stream (11) and / or ii) at least a portion of the first oxygen enriched stream (12).

10. The process according to any one of claims 8-9, wherein the temperature of at least one of i) at least a portion of the carbon monoxide-rich stream (11) and / or ii) at least a portion of the first oxygen enriched stream (12) is / are in the range of 200-500 °C and the pressure of at least one of i) at least a portion of the carbon monoxide-rich stream (11) and / or ii) at least a portion of the first oxygen enriched stream (12) is / are in the range of 0 - 3 bar g.

11. The process according to any one of claims 8-10, wherein the first solid oxide electrolysis (SOE) section (10) operates in the temperature range of 500-900 °C, preferably 700-800 °C.

12. The process according to any one of claims 8-11, wherein the second electrolysis section is a solid oxide electrolysis (SOE) section operating in the temperature range of 500- 900 °C, preferably 700-800 °C.

13. The process according to any one of claims 8-12, wherein the temperature of the first steam stream (13) is between 100 - 210 °C, preferably 150 - 180 °C and wherein the pressure of the first steam stream (13) is between 3.5 - 9 bar g.

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