Plasma-assisted methanol synthesis process

Abstract

A process to produce methanol from a CO2-containing stream (13), the process comprising: a) providing a feedstream (11) comprising carbon dioxide and hydrogen, b) performing a Reverse Water-Gas Shift (RWGS) reaction on said feedstream (11) to obtain a syngas (21), c) drying the syngas (21) to obtain a dried syngas (25); and d) submitting the dried syngas to a methanol synthesis reaction to obtain a first methanol-containing stream (29); wherein the RWGS reaction is performed by plasma catalysis at a temperature below 450°C, wherein the plasma catalysis comprises generating a plasma in one or more dielectric barrier discharge (DBD) reactors in the presence of a first catalytic composition (19).

Description

[0001]PLASMA-ASSISTED METHANOL SYNTHESIS PROCESSTechnical fieldThe present disclosure invention relates to a methanol synthesis process.Technical background 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 dimethylether, 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. Methanol is commercially produced from synthesis gas (syngas), i.e., a mixture of carbon oxide (i.e., carbon monoxide (CO) and / or carbon dioxide (CO2)) and hydrogen (H2) that can be produced from a variety of carbonated sources. CO and CO2react with H2according to the following equations: CO+2H2═CH3OH (1) CO2+3H2=CH3OH+H2O (2) CO+H2O=CO2+H2 (3) wherein the third one corresponds to the water-gas shift (WGS) reaction. The increasing concentration of carbon dioxide (CO2) in the atmosphere, primarily due to the combustion of fossil fuels, is a significant driver of climate change. This has spurred considerable interest in technologies that can reduce CO2emissions. One such promising technology is the methanol synthesis reaction, which converts CO2and hydrogen into methanol. Methanol is a versatile chemical that can be used as a fuel, a fuel additive, or a feedstock for producing various chemicals and materials. The methanol synthesis process not only provides a valuable use for captured CO2but also offers a way to store and transport renewable energy, as hydrogen can be produced from water electrolysis using renewable energy sources. By integrating CO2capture and utilization with methanol synthesis, it is possible to create a sustainable and circular carbon economy. This process can be optimized to enhance efficiency and reduce costs, making it an attractive solution for large-scale CO2emission reduction.Document CN 111548251 A discloses a method for preparing methanol by methane all-component low-temperature plasma catalysis, which comprises the following steps: mixing desulfurized methane with water vapor to obtain mixed gas, carrying out a reaction in a low- temperature plasma reactor at 200-300 °C under normal pressure in the presence of a catalystto obtain synthetic gas, and preparing methanol by converting methane and carbon dioxideinto synthesis gas at atmospheric pressure and low temperature.There is still a need for processes to produce synthetic methanol that allows for a reduction ofthe carbon footprint, such as enabling direct utilisation of CO2. Summary of the disclosure It has now been found that one or more of the above needs can be fulfilled by the use of plasmacatalytic reactions to produce the syngas used in a methanol synthesis process.According to a first aspect, the disclosure provides for a process to produce methanol from aCO2-containing stream, the process comprising: a) providing a feedstream comprising carbon dioxide and hydrogen, wherein the molarratio of hydrogen to carbon dioxide in the feedstream ranges from 4:1 to 1:1;b) performing a Reverse Water-Gas Shift (RWGS) reaction on said feedstream toobtain a syngas, c) drying the syngas to obtain a dried syngas; andd) submitting the dried syngas to a methanol synthesis reaction to obtain a firstmethanol-containing stream;wherein the process is remarkable in that in step b), the RWGS reaction is performed byplasma catalysis at a temperature below 450°C, wherein the plasma catalysis comprises generating a plasma in one or more dielectric barrier discharge (DBD) reactors in the presence of a first catalytic composition.For example, each of the RWGS reaction and the methanol synthesis reaction are performedat a temperature of at most 350°C; with preference at most 300°C; more preferably at most 280°C. As it is understood from the definition given, the process provides for an integrated methanolsynthesis process wherein the syngas is produced from a CO2 stream using a plasma-activated RWGS reaction. The process is remarkable in that it allows for full electrification ofthis part of the process; enables fast start / stop; and requires less heat than conventionalsolutions. Dielectric barrier discharge (DBD) reactors are known to the person skilled in the art. For example, WO2021 / 255423 describes an apparatus for forming a C1 to C5 oxygenate from carbon dioxide and a C1 to C4 hydrocarbon. The apparatus comprises: a dielectric barrier discharge, DBD, device arranged to generate a plasma; and a passageway having an inlet for the carbon dioxide and the C1 to C4 hydrocarbon and an outlet for the oxygenates. In one example the passageway includes therein a catalyst. The passageway extends, at least in part, through the DBD device wherein, in use, the carbon dioxide in reacted with the C1 to C4 hydrocarbon in the generated plasma, thereby forming the oxygenates from at least some of the carbon dioxide and the C1 to C4 hydrocarbon. One or more of the following can be used to further describe the first catalytic composition.For example, the first catalytic composition comprises at least an active component whereinthe active component comprises one or more selected from Ni, Fe, Co, Mo, Cu, Au, Ru, Rh,Re, Pd, Ir, Pt, Mn, La, W, Cr, Zn, Y, Zr, Ag, Li, Na, K, Rb, Cs, Mg, Ca, Ce, La, Sc, and Y. Withpreference, the first catalytic composition comprises at least an active component wherein theactive component is or comprises one or more selected from Ni, Fe, Co, Mo, and Cu.For example, the first catalytic composition comprises an active component comprising one or more metallic compounds selected from: -one or more non-noble metals selected from Ni, Fe, Co, Mo, Cu, and any mixturethereof; -one or more noble metals selected from Au, Ru, Rh, Re, Pd, Ir, Pt, and any mixturethereof; and -one or more bimetallic compounds comprising a non-noble metal and a noble metalwherein the non-noble metal is selected from Ni, Fe, Co, Mo, and Cu, and the noblemetal is selected from Au, Ru, Rh, Re, Pd, Ir and Pt;with preference, the active component of the first catalytic composition is or comprises Niand / or Co. In an embodiment, the first catalytic composition comprises an active component comprising Fe and / or Cu.In an embodiment, the first catalytic composition comprises an active component Fe and atleast one metallic compound from Ni, Co, Mo, Cu.For example, the first catalytic composition comprises a catalyst support selected from ZrO2,Al2O3, MgO, SiO2, Al2O3-ZnO, CeO2, TiO2, and any mixture thereof; with preference the catalyst support is or comprises Al2O3 and / or MgO. In an embodiment, the first catalytic composition comprises an active component Fe and atleast one metallic compound from Ni, Co, Mo, Cu; and a catalyst support comprising Al2O3and / or MgO. For example, the first catalytic composition comprises one or more selected fromNi / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Ni / MgO, Ni / SiO₂, Cu / ZnO-Al₂O₃, Cu / SiO₂, Fe / Al₂O₃, Fe / CeO₂, Co / Al₂O₃, Co / SiO₂, CoxOy / MgO, La1-xSrxNiyFeyO3+δ; with preference, selected from Ni / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Fe / Al₂O₃, Co / Al₂O₃, CoxOy / MgO, and La1-xSrxNiyFeyO3+δ;more preferably, selected from Fe-Cu / Al₂O₃, Ni / Al₂O₃, Co / Al₂O₃, Fe / Al₂O₃, CoxOy / MgO, andLa1-xSrxNiyFeyO3+δ; even more preferably Fe-Cu / Al₂O₃, In an embodiment, the RWGS reaction by plasma catalysis is performed at a temperature ranging from 150°C to 300°C; preferably from 200°C to 270°C. In an embodiment, the molar ratio of hydrogen to carbon dioxide in the feedstream is ranging from 4:1 to 2:1, preferably from 3:1 to 2:1 In an embodiment, the discharge frequency ranges from 50 to 100 kHz and / or the electrical power supplied ranges from 20 to 40 W. In an embodiment, step c) drying the syngas is performed by sorbents, membrane separation, condensation, cryogenic distillation, or any combination thereof. In an embodiment, the drying step further includes a sub-step of adjusting the hydrogen content of the syngas and / or of the dried syngas to obtain a hydrogen-to-carbon monoxide molar ratio of at least 2:1. In an embodiment, the drying step comprises a step of CO2removal; preferably the step of CO2removal is performed by condensation or by cryogenic distillation. In an embodiment, the methanol synthesis is performed at a temperature ranging from 180 to 350°C, using a second catalytic composition that is or comprises one or more selected from acopper zinc oxide catalyst, an indium oxide catalyst, Cu-ZnO / Al2O3, Cu-ZnO-Ga2O3 / SiO2, Cu-ZnO-Al2O3 / ZrO2, ZnO, Au / ZnO, Au / Fe2O3, Au / TiO2, Au / ZrO2, Au / La2O3, Au / ZnFe2O4, Fe2O3, Au / Fe2O3, Cu / ZnO, CeO2, TiO2, ZrO2, La2O3, Zn / Fe2O3, and a combination thereof; preferably at a pressure ranging between 5.0 and 10.0 MPa. In an embodiment, the process further comprises a step e) of separation of the first methanol- containing stream comprising first sub-step e1) of condensation resulting in a non-condensable gas stream and a second methanol-containing stream. With preference, the process further comprises recycling the non-condensable gas stream into the feedstream provided in step a). With preference, the step e) of separation of the first methanol-containing stream comprises a second sub-step e2) of distillation that is performed on the second methanol-containing stream to obtain methanol stream.According to a second aspect, the disclosure provides for an installation to carry out theprocess according to the first aspect remarkable in that it comprises, in the following order:- an RWGS unit comprising at least one plasma catalytic reactor;- a drying unit; and- a methanol synthesis unit comprising one or more reactors;with preference, the installation further comprises a CO2-H2blending zone and / or a separation unit. Description of the figures -Figure 1 illustrates an example of installation to conduct the disclosed processDetailed descriptionFor the disclosure, the following definitions are given. 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 notexclude additional, non-recited members, elements or method steps. The terms "comprising”,"comprises" and "comprised of" also include the term “consisting of”. The recitation of numerical ranges by endpoints includes all integer numbers and, where appropriate, fractions subsumed within that range (e.g., 1 to 5 can include 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. As used herein, the term “C# hydrocarbons”, wherein “#” is a positive integer, is meant to describe all hydrocarbons having # carbon atoms. C# hydrocarbons are sometimes indicated as just C#. Moreover, the term “C#+ hydrocarbons” is meant to describe all hydrocarbon molecules having # or more carbon atoms. Accordingly, the expression “C10+ hydrocarbons” is meant to describe a mixture of hydrocarbons having 10 or more carbon atoms. The metals Au, Ag, Ru, Rh, Pd, Os, Ir and Pt show outstanding oxidation resistance and are considered “noble” metals. Other metals can be considered as “non-noble” metals.The term “alkali metal” refers to an element classified as an element from group 1 of theperiodic table of elements (or group IA), excluding hydrogen. According to this definition, the alkali metals are Li, Na, K, Rb, Cs and Fr.The term “alkaline earth metal” refers to an element classified as an element from group 2 ofthe periodic table of elements (or group IIA). According to this definition, the alkaline earth metals are Be, Mg, Ca, Sr, Ba and Ra. The term “rare earth elements” refer to the fifteen lanthanides, as well as scandium and yttrium. The 17 rare-earth elements are cerium (Ce), dysprosium (Dy), erbium (Er), europium (Eu), gadolinium (Gd), holmium (Ho), lanthanum (La), lutetium (Lu), neodymium (Nd), praseodymium (Pr), promethium (Pm), samarium (Sm), scandium (Sc), terbium (Tb), thulium (Tm), ytterbium (Yb), and yttrium (Y).The term "DBD- dielectric barrier discharge" describes an electrical discharge created betweentwo electrically conductive elements separated by one or more dielectric elements. The term "dielectric" describes an electrically insulating material that provides electrical insulation. The process and the installation to conduct the process will be jointly described with reference to Figure 1.The present disclosure provides a process to produce methanol from a CO2-containing stream13, the process comprising a) providing a feedstream 11 comprising carbon dioxide and hydrogen,b) performing a Reverse Water-Gas Shift (RWGS) reaction on said feedstream 11 to obtain a syngas 21, c) drying the syngas 21 to obtain a dried syngas 25; and d) submitting the dried syngas to a methanol synthesis reaction to obtain a firstmethanol-containing stream 29; wherein the process is remarkable in that in step b), the RWGS reaction is performed by plasma catalysis at a temperature below 450°C, wherein the plasma catalysis comprises generating a plasma in one or more dielectric barrier Discharge (DBD) reactors 5 in the presence of a first catalytic composition.For example, each of the RWGS reaction and the methanol synthesis reaction are performedat a temperature of at most 350°C; with preference at most 300°C; more preferably at most 280°C.The present disclosure provides an installation 1 to perform the process of the disclosure,wherein the installation 1 comprises in the following order:- a RWGS unit 3 comprising at least one plasma catalytic reactor 5;- a drying unit 7; and- a methanol synthesis unit 9 comprising at least one reactor.The drying unit is placed downstream from the RWGS unit 3 and the methanol synthesis unit9 is placed downstream from the drying unit 7.The feedstream and the step a) of providing a feedstreamThe feedstream 11 provided in step a) comprises carbon dioxide and hydrogen. The feedstream 11 is gaseous. In an embodiment the molar ratio of hydrogen to carbon dioxide in the feedstream is rangingfrom 5:1 to 1:1, preferably from 4:1 to 1:1 or from 4:1 to 2:1; more preferably from 3.5:1 to1.5:1; even more preferably from 3:1 to 2:1. Hydrogen is provided as a hydrogen stream 15 and can be produced by any means known to the skilled person, including electrolysis of water, steam reforming of natural gas followed by a step for pressure Swing adsorption (PSA) separation, or by temperature Swing adsorption (TSA), or by membrane separation. The CO2 is provided as CO2-containing stream 13 can be of any origin and is preferentially obtained by CO2 capture. The CO2-containing stream 13, the hydrogen stream 15, and an optional non-condensable gasstream 35 are blended directly in the one or more DBD reactors or in an CO2-H2 blending zone17 placed before the one or more DBD reactors. In a preferred embodiment, the different gasstream are blended before being fed into the one or more dielectric barrier Discharge (DBD)reactors 5.The installation 1 may comprise a CO2-H2 blending zone 17 to prepare the feedstream 11. TheCO2-H2 blending zone 17 can be in the fed lines or can be a blending vessel. In such a casethe vessel of the CO2-H2 blending zone 17 comprises at least two inputs and one output. Acarbon dioxide-containing stream 13 is connected to a first input while a hydrogen stream 15 is connected to a second input. In a preferred embodiment, a third input is provided to recyclea non-condensable gas stream 35 coming from a separation unit 31. The feedstream 11 exitsthe CO2-hydrogen blending zone 17 through the output and is directed towards an RWGS unit3 comprising one or more plasma catalytic reactors 5. The step b) of performing a Reverse Water-Gas Shift (RWGS) reaction The Reverse Water-Gas Shift (RWGS) reaction is a chemical process that converts carbon dioxide (CO2) and hydrogen (H2) into carbon monoxide (CO) and water (H2O). The reaction is represented by the following equation: CO2+ H2→ CO + H2O According to the present disclosure, the RWGS reaction is performed by plasma catalysis at a temperature below 450°C, wherein the plasma catalysis comprises generating a plasma in adielectric barrier Discharge (DBD) reactor 5 in the presence of a first catalytic composition 19.For example, the RWGS reaction by plasma catalysis is performed at a temperature ranging from 100°C to 450°C; preferably from 110°C to 400°C; more preferably from 120°C to 350°C, even more preferably from 140°C to 320°C, even more preferably from 150°C to 300°C; even more preferably from 160°C to 290°C; most preferably from 180°C to 280°C, and most preferably from 200°C to 270°C. For example, the RWGS reaction by plasma catalysis is performed at a temperature of at most 450°C; preferably, at most 400°C; more preferably, at most 350°C, even more preferably, at most 320°C, even more preferably, at most 300°C; even more preferably, at most 290°C; most preferably, at most 280°C, and most preferably, at most 270°C. For example, the RWGS reaction by plasma catalysis is performed at a temperature of at least 100°C; preferably at least 110°C; more preferably at least 120°C, even more preferably at least140°C, even more preferably at least 150°C; even more preferably at least 160°C; mostpreferably at least 180°C, and most preferably at least 200°C. The DBD reactor DBD reactors are well known to the person skilled in the art. An example of a DBD reactor is described in WO2023 / 037258 which is incorporated by reference. A dielectric Barrier Discharge (DBD) reactor 5 is an apparatus designed to generate non- thermal plasma. It comprises high-voltage electrodes. A first catalyst composition 19 is placed between the electrodes, allowing the feedstream 11 that is gaseous to contact the catalyst composition 19. The catalyst composition 19 is provided in the form of a fixed bed in a catalyst- holding element that is made of a dielectric material and is inserted in the plasma dischargezone whilst allowing the feedstream 11 to flow through it. The catalyst composition 19 isactivated by a plasma generated from high-voltage electrical discharges (of the order of kV). This polarization gives rise to the formation of plasma, as well as the catalyst composition 19 activation and the RWGS reaction. The product stream obtained in this step is a syngas 21 comprising carbon monoxide, water, carbon dioxide, and hydrogen.For example, the discharge frequency ranges from 50 to 100 kHz, and / or the electrical powersupplied ranges from 20 to 40 W. The first catalytic composition The first catalytic composition comprises at least an active component. For example, the first catalytic composition comprises an active component and a catalytic support. In an embodiment, the first catalytic composition 19 comprises at least an active componentwherein the active component comprises one or more selected from Ni, Fe, Co, Mo, Cu, Au,Ru, Rh, Re, Pd, Ir, Pt, Mn, La, W, Cr, Zn, Y, Zr, Ag, Li, Na, K, Rb, Cs, Mg, Ca, Ce, La, Sc, and Y. In an embodiment, the first catalytic composition 19 comprises at least an active component selected from Ni, Fe, Co, Mo, Cu, Au, Ru, Rh, Re, Pd, Ir, Pt, Mn, La, W, Cr, Zn, Y, Zr, Ag, Li,Na, K, Rb, Cs, Mg, Ca, Ce, La, Sc, Y, and any mixture thereof.For example, the first catalytic composition 19 comprises at least an active component comprising a metallic compound selected from: Ni, Fe, Co, Mo, Cu, Au, Ru, Rh, Re, Pd, Ir, Pt,Mn, La, W, Cr, Zn, Y, Zr, Ag, and any mixture thereof; with preference, Ni, Fe, Co, Mo, Cu, Au,Ru, Rh, Re, Pd, Ir, Pt, and any mixture thereof; more preferably, Ni, Fe, Co, Mo, Cu, and anymixture thereof.In an embodiment, the first catalytic composition 19 comprises at least an active componentcomprising a metallic compound selected from Mn, La, W, Cr, Zn, Y, Zr, Ag, and any mixturethereof. In an embodiment, the first catalytic composition 19 comprises at least an active component comprising a metallic compound selected from: -one or more non-noble metals selected from Ni, Fe, Co, Mo, Cu, and any mixture thereof;- one or more noble metals selected from Au, Ru, Rh, Re, Pd, Ir, Pt, and any mixture thereof;and- one or more bimetallic compounds comprising a non-noble metal and a noble metalwherein the non-noble metal is selected from Ni, Fe, Co, Mo, and Cu, and the noble metalis selected from Au, Ru, Rh, Re, Pd, Ir, and Pt.For example, the one or more non-noble metals selected from Ni, Fe, Co, Mo, Cu and any mixture thereof are present in an amount ranging between 0.05 wt.% and 20.00 wt.% based on the total weight of the first catalytic composition, preferably between 0.10 wt.% and 15.00 wt.%, more preferably between 0.50 wt.% and 10.00 wt.%, even more preferably between 1.00 wt.% and 5.00 wt.%. For example, the one or more non-noble metals are or comprise Ni and / or Co. For example, the one or more noble metals selected from Au, Ru, Rh, Re, Pd, Ir, Pt and any mixture thereof are present in an amount ranging between 0.05 wt.% and 10.00 wt.% based on the total weight of the first catalytic composition, preferably between 0.10 wt.% and 5.00 wt.%, more preferably between 1.00 wt.% and 3.00 wt.%, even more preferably between 1.50 wt.% and 2.50 wt.%. For example, the one or more noble metals are or comprise Ru, preferably in an amount ranging between 0.05 wt.% and 10.00 wt.% based on the total weight of the first catalytic composition. In a preferred embodiment, the active component of the first catalytic composition comprises Ni and / or Co. For example, the one or more non-noble metals are or comprise Fe and / or Cu. For example, the one or more non-noble metals are or comprise Mo. In an embodiment, the first catalytic composition comprises an active component Fe and atleast one metallic compound from Ni, Co, Mo, Cu.With preference, the first catalytic composition comprises one or more composite oxides selected from: -CuO / ZnO / Al2O3, NiO / CeO2, ZnO / Al2O3, ZnO / Cr2O3, CuOx / CeO2, In2O3-CeO2, FeOx,CoxOy, CoxOy / MgO, or any combinations thereof; -spinel oxides such as ZnAl2O4, ZnCr2O4, CuAl2O4, CoAl2O4, or any combinationsthereof; -solid solution oxides, such as ZnxZr1−xO2−y, CexZr1−xO2−y, or any combinations thereof(wherein x is ranging between 0 and 0.5 and / or wherein y is ranging between 0 and 0.5)- and perovskite-type oxides, such as BaZr1−x-yYxZnyO3−δ, La1-xSrxCoO3−δ, La1-xSrxFeO3−δ,LaNiO3, La1-xSrxNiO3+δ, La1-xSrxFeO3−δ, SrCe1-xYxO3−δ, La1-xSrxNiyFeyO3+δ, or any combinations thereof (wherein x is ranging between 0 and 0.5 and / or wherein y is ranging between 0 and 0.5 and / or wherein d is ranging between 0 and 0.5). In an embodiment, the first catalyst composition comprises CoxOy / MgO, La1-xSrxNiyFeyO3+δ, or any mixture thereof; preferably wherein La1-xSrxNiyFeyO3+δ, is La0.9Sr0.1Ni0.5Fe0.5O3+ δ.In an embodiment, the first catalytic composition 19 comprises at least an active componentcomprising a compound selected from Li, Na, K, Rb, Cs, Mg, Ca, Ce, La, Sc, Y, and anymixture thereof. Advantageously, said first catalytic composition 19 further comprises one or more elementsselected from one or more selected from alkali metals, alkaline earth metals, and rare earthelements. For example, one or more alkali metals are one or more selected from Li, Na, K, Rb,Cs, and any mixture thereof; with preference, Li, Na, K, Cs, and any mixture thereof. Forexample, one or more alkaline earth metals are one or more selected from Mg and / or Ca. Forexample, one or more rare earth elements are one or more selected from Ce, La, Sc, Y, andany mixture thereof. More preferably, the first catalytic composition comprises Ce.For example, the active component of the first catalytic composition comprises Ce and oneselected from Ni, Co, and any mixture thereof.In a preferred embodiment, the active component of the first catalytic composition comprisesFe and / or Cu.With preference, said first catalytic composition further comprises a catalytic support.Suitable particulate catalytic supports can be selected from refractory oxides such as alumina(Al2O3, g-Al2O3, b-Al2O3, h-Al2O3, d-Al2O3, amorphous Al2O3), silica (SiO2), titania (TiO2), ceria(CeO2), zirconia (ZrO2), magnesia (MgO), yttria (Y2O3), hafnia (HfO2), lanthania (La2O3), niobium oxide (Nb2O3), tungsten oxide and any mixture thereof.Suitable particulate catalytic supports can be selected from mixed oxides such as SiO2-Al2O3,SiO2-TiO2, SiO2-SnO2, SiO2-ZrO2, SiO2-BeO, SiO2-MgO, SiO2-CaO, SiO2-SrO, SiO2-ZnO, SiO2-Ga2O3, SiO2-Y2O3, SiO2-La2O3, SiO2-WO3, SiO2-ThO2, Al2O3-MgO, Al2O3-ZnO, Al2O3- ThO2, AI2O3-TiO2, Al2O3-ZrO2, Al2O3-MoO3, AI2O3-WO3, Al2O3-Cr2O3, Al2O3-Mn2O3, Al2O3- Fe2O3, TiO2-MgO, TiO2-ZnO, TiO2-ZrO2, TiO2-SnO2, TiO2-Sb2O5, TiO2-V2O5, TiO2-Cr2O3, TiO2- MoO3, TiO2-WO3, WO3-ZrO2, Nb2O5-Al2O3, Nb2O5-WO3, Nb2O5-MoO3, Nb2O5-ZrO2, Nb2O5- TiO2, TiO2-Fe2O3, CeO2-ZrO2, MgAl2O3, CaAl2O3and mixtures thereof.Suitable particulate catalytic supports for the metallic compounds can be selected from one ormore carbon-containing carriers, such as graphite, graphene, carbon nanotubes, char, charcoal, black carbon, petcoke, siliconcarbide, boroncarbide, ironcarbide (FexC), molybdynum carbide (MoxC), titaniumcarbide (TiC) and or mixtures thereof. Suitable catalytic support can be selected from zeolites or molecular sieves having 8, 10 or 12-membered rings. With preference, the one or more zeolites or molecular sieves are selected from CHA (such as chabazite, SAPO-34), ERI (erionite), FAU (such as zeolite Y, X or USY), BEA (such as zeolite beta), MFI (such as ZSM-5), MEL (such as ZSM-11), MOR (such as mordenite), FER (such as ferrierite), MTT, MWW, TON, EUO, HEU, MFS, and MRE families, and any combinations thereof. For example, the catalyst support is selected from ZrO2, Al2O3, MgO, SiO2, Al2O3-ZnO, CeO2, TiO2, and any mixture thereof. With preference, the catalyst support is or comprises CeO2,Al2O3, MgO, and any mixture thereof. More preferably, the catalyst support is or comprisesAl2O3. In an embodiment, the first catalytic composition comprises an active component Fe and atleast one metallic compound from Ni, Co, Mo, Cu; and a catalyst support comprising Al2O3and / or MgO. In an embodiment, the first catalyst composition 19 consists in or comprises one or moreselected from Ni / Al₂O₃, Ni / MgO, Ni / SiO₂, Cu / ZnO-Al₂O₃, Cu / SiO₂, Fe / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Fe / CeO₂, Fe-Cu / CeO₂, Cu / CeO₂, Co / Al₂O₃, Co / SiO₂, Ru / Al₂O₃, Ru / TiO₂, Pd / CeO₂,Pd / Al₂O₃, Au / TiO₂, Au / CeO₂, Pt / Al₂O₃, Pt / CeO₂, Fe / Al₂O₃, Fe / CeO₂. Fe / La2O3, Cu / La2O3, Fe-Cu / La2O3, Fe / Y2O3, Cu / Y2O3, Fe-Cu / Y2O3.Preferably, the first catalyst composition consists in or comprises one or more selected from Ni / Al₂O₃, Ni / MgO, Ni / SiO₂, Cu / ZnO-Al₂O₃, Cu / SiO₂, Fe / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Fe / CeO₂, Co / Al₂O₃, Co / SiO₂, Ru / Al₂O₃, Ru / TiO₂, Pd / CeO₂, Pd / Al₂O₃, Au / TiO₂, Au / CeO₂,Pt / Al₂O₃, Pt / CeO₂, Re / Al₂O₃, Re / CeO₂. More preferably, the first catalyst composition consistsin or comprises one or more selected from Ni / Al₂O₃, Ni / MgO, Ni / SiO₂, Cu / ZnO-Al₂O₃, Cu / SiO₂, Fe / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Fe / CeO₂, Co / Al₂O₃, Co / SiO₂. Even more preferably, the first catalyst composition consists in or comprises one or more selected from Co / Al₂O₃, Ni / Al₂O₃, Fe / Al₂O₃, Fe-Cu / Al₂O₃, and any mixture thereof; and most preferably, Fe-Cu / Al₂O₃. With preference, said first catalytic composition 19 further comprises a specific surface area ranging between 10 m2 / g and 1000 m2 / g as determined by N2adsorption measurement, more preferably between 50 m2 / g and 900 m2 / g, even more preferably between 100 m2 / g and 800 m2 / g, most preferably between 200 m2 / g and 700 m2 / g. Examples of suitable catalysts are described in the below references, which are all incorporated by reference: ^Liu et al. in “Low-temperature catalytic reverse water-gas shift reaction over perovskitecatalysts in DBD plasma” - Applied Catalysis B: Environmental 265 (2020) 11857.^ Yuxuan Zeng and Xin Tu in “Plasma-catalytic hydrogenation of CO2 for thecogeneration of CO and CH4 in a dielectric barrier discharge reactor: effect of argonaddition” - J. Phys. D: Appl. Phys.50 (2017) 184004^ Ronda-Lioret et al in “CO2 Hydrogenation at Atmospheric Pressure and LowTemperature Using Plasma-Enhanced Catalysis over Supported Cobalt Oxide Catalysts) - ACS Sustainable Chem. Eng. , 8, (2020)47, 17397–17407The step c) of drying the syngas to produce a dried syngas The syngas 21 obtained from the RWGS reaction comprises water 23 and therefore must bedried before being subjected to the methanol synthesis reaction. The drying of the syngas 21to obtain a dried syngas 25 can be done by any means, in a drying unit 7. In an embodiment, the drying step is performed by sorbents, membrane separation, condensation, cryogenic distillation, or any combination thereof. Any suitable sorbent capable of adsorbing water can be used. Silica, silica gel, or molecular sieves such as 13X or any mixture thereof can for instance be used to dry the syngas. In a preferred embodiment, the step of drying is performed until the content of water is at most5.0 vol.-%, preferably at most 3.0 vol. %, more preferably at most 1.0 vol.% of H2O based onthe total volume of the dried syngas 25. In an embodiment, the drying step comprises a step of CO2 removal. The drying step and theCO2 removal step (i.e. the purification step) are preferably done consecutively (in successivesub-steps). For example, the step of step of CO2 removal is performed by condensation or bycryogenic distillation. An example of a process of drying and purification of syngas by CO2removal by cryogenic distillation is described in WO2006079736 which is incorporated byreference. When the step of CO2 removal is performed, the CO2 recovered is preferablyrecycled in the feedstream 11. In an embodiment, the drying step further includes a sub-step of adjusting the hydrogen content of the syngas 21 and / or of the dried syngas 25 to obtain a hydrogen-to-carbon monoxide molar ratio of at least 2:1. Adjusting the content can be obtained by adding hydrogen to the syngas 21 and / or of the dried syngas 25.In a preferred embodiment, the drying step further includes a sub-step of adjusting the pressurethe syngas 21 and / or of the dried syngas 25 before entering the methanol synthesis unit 9.The pressure is preferably adjusted to range from 2.0 to 15.0 MPa, preferably from 3.0 to 14.0MPa, more preferably from 4.0 to 12.0 MPa, even more preferably from 4.5 to 11.0 MPa, andmost preferably from 5.0 to 10.0 MPa. In such a case the installation further comprises at leastone compressor 47 that is placed upstream of the methanol synthesis unit 9.The dried syngas 25 is then fed to the methanol synthesis unit 9 comprising one or morereactors.The step d) of Methanol synthesisMethanol synthesis from syngas is performed using a catalytic reaction. Methanol synthesis is performed in a methanol synthesis unit 9 comprising one or morereactors. With preference, the one or more reactors are fixed-bed reactors or fluidized-bedreactors comprising at least one catalytic bed. Such reactors are well-known by the personskilled in the art and for instance, described in EP2257366 or US7279138 which areincorporated by reference. In case the methanol synthesis unit 9 comprises more than onereactor, the second catalytic composition 27 is present at least in the first reactor. The catalyticcomposition used in the one or more subsequent reactors can be the same as the secondcatalytic composition or can be different.The methanol synthesis reaction is performed under reaction conditions that comprisetemperature conditions between 180°C and 350°C, preferably between 190°C and below 340°C; preferably between 200°C and 320°C; more preferably between 210°C and 300°C, even more preferably between 220°C and 280°C.The methanol synthesis reaction is performed using a second catalytic composition 27. Thesecond catalytic composition may comprise any catalyst suitable for methanol synthesis. The second catalytic composition 27 comprises an active component and an optional catalytic support.For example, the second catalytic composition 27 is or comprises one or more selected froma copper zinc oxide catalyst, an indium oxide catalyst, Cu-ZnO / Al2O3, Cu-ZnO-Ga2O3 / SiO2,Cu-ZnO-Al2O3 / ZrO2, ZnO, Au / ZnO, Au / Fe2O3, Au / TiO2, Au / ZrO2, Au / La2O3, Au / ZnFe2O4, Fe2O3,Au / Fe2O3, Cu / ZnO, CeO2, TiO2, ZrO2, La2O3, Zn / Fe2O3, and a combination thereof; preferablyselected from an indium oxide catalyst, Cu-ZnO / Al2O3, Cu-ZnO-Ga2O3 / SiO2, Cu-ZnO-Al2O3 / ZrO2, ZnO, Au / ZnO, Au / Fe2O3, Au / TiO2, Au / ZrO2, Au / La2O3, Au / ZnFe2O4, Fe2O3,Au / Fe2O3, Cu / ZnO, CeO2, TiO2, ZrO2, La2O3, Zn / Fe2O3, and a combination thereof; preferably,selected from Cu-ZnO / Al2O3, Cu-ZnO-Ga2O3 / SiO2, and Cu-ZnO-Al2O3 / ZrO2, more preferably selected from Cu-ZnO-Al2O3 / ZrO2.For example, the catalyst support of the second catalytic composition 27 comprises at leastone selected from silica (SiO2), alumina (Al2O3), gallium oxide (Ga2O3), cerium oxide (CeO2), vanadium oxide (V2O5), chromium oxide (Cr2O3), zirconium dioxide (ZrO2), titanium dioxide (TiO2), magnesium oxide (MgO), zinc oxide (ZnO), tin oxide (SnO2), carbon black (C), andcombinations thereof. Preferably, the catalyst support of the second catalytic composition 27comprises at least one selected from zinc oxide (ZnO), zirconium dioxide (ZrO2) and titaniumdioxide (TiO2) or a combination thereof; and more preferably the catalyst support of the secondcatalytic composition 27 is or comprises zirconium dioxide. When the catalyst supportcomprises zirconium dioxide (ZrO2), the zirconium dioxide can be monoclinic, tetragonal, or cubic.In an embodiment, the catalyst support of the second catalytic composition 27 is zirconiumdioxide or a combination of zirconium dioxide with another catalyst support in which zirconiumdioxide is comprised in an amount of at least 10 wt.%, preferably at least 50 wt.%, morepreferably at least 80 wt.%, and even more preferably at least 90 wt.% based on the totalweight of the catalyst support, the other catalyst support is selected from silica (SiO2), alumina(Al2O3), gallium oxide (Ga2O3), cerium oxide (CeO2), vanadium oxide (V2O5), chromium oxide (Cr2O3), titanium dioxide (TiO2), magnesium oxide (MgO), zinc oxide (ZnO), tin oxide (SnO2), carbon black (C), and combinations thereof; preferably the other catalyst support is selected from zinc oxide (ZnO), titanium dioxide (TiO2), and combinations thereof.The catalyst support of the second catalytic composition 27 can be porous or non-porous. Insome embodiments, the catalyst support of the second catalytic composition 27 is provided ina particulate form of particles having a surface area (i.e., BET surface area) as determined byN2 sorption analysis according to ASTM D3663 – 03, in the range of about 5 m2 g-1 to about400 m2 g-1, such as from 30 m2 g-1 to about 200 m2 g-1, and / or with a pore volume in the rangeof about 0.1 cm3g-1to about 10 cm3g-1, such as from about 0.2 cm3g-1to about 5 cm3g-1.The second catalytic composition 27 can be a calcined supported catalyst and has preferablya surface area (i.e BET surface area) as determined by N2 sorption analysis according to ASTMD3663 – 03, in the range of about 5 m2g-1 to about 400 m2 g-1, such as from 30 m2 g-1 to about200 m2g-1.When no CO2 removal step is performed, the person killed in the art may select a secondcatalytic composition 27 being susceptible to resist a high concentration of carbon dioxide. Forexample, it may be advantageous that second catalytic composition 27 comprises or is acopper zinc oxide catalyst or an indium oxide catalyst, preferably a copper zinc oxide catalyst. With respect to indium oxide catalysts, upon standard reaction conditions, they are not deactivated when being in the presence of a high concentration of carbon dioxide. Similar behaviour is observed when copper zinc oxide catalysts have been used. Advantageously, indium oxide catalyst can further comprise a catalyst support. Indium oxide in the form of In2O3deposited on a catalyst support and their method of preparation are known and described for example in WO2017 / 118572 and in WO2017 / 118573 which are incorporated by reference. The copper zinc oxide catalystIt is preferred that the second catalytic composition 27 is or comprises a copper zinc oxidecatalyst. Wherein the catalytic composition 27 is or comprises a copper zinc oxide catalyst, itis preferred that the temperature conditions range from for example between 180°C and 300°C, preferably between 180°C and 280°C; more preferably, between 185°C and 270°C, even more preferably between 190°C and 250°C; most preferably, between 190°C and 240°C, even most preferably between 200°C and 235°C. For example, the temperature conditions are at least 180°C, preferably at least 190°C, andmore preferably at least 200°C. For example, the temperature conditions are at most 300°C,or at most 280°C, preferably at most 270°C or at most 250°C; more preferably at most 245°Cor at most 240°C, even more preferably at most 235°C.The temperature conditions are the start-of-run temperature conditions. For example, said copper zinc oxide catalyst is selected from Cu / ZnO, Cu-ZnO / Al2O3, Cu-ZnO-Ga2O3 / SiO2, Cu-ZnO-Al2O3 / ZrO2 and any mixture thereof; preferably said copper zinc oxidecatalyst is or comprises Cu-ZnO-Al2O3 / ZrO2.The copper-zinc oxide catalyst can be activated, preferably by reduction with hydrogen. Saidcopper zinc oxide catalyst is advantageously prepared by co-precipitation. For example, saidcopper zinc oxide catalyst is an activated supported catalyst and / or has a surface area in therange of about 5 m2g-1to about 400 m2g-1, such as from 30 m2g-1to about 200 m2g-1as determined according to N2sorption analysis according to ASTM D3663-03. The indium oxide For example, the second catalytic composition 27 is or comprises an indium oxide catalyst.For example, the indium oxide catalyst is under the form of In2O3. The use of an indium oxide catalyst is advantageous in case CO2is present in the dried syngas. In case the methanolsynthesis unit 9 comprises more than one reactors, the second catalytic composition 27comprising an indium oxide catalyst is preferably present at least in the first reactor. WO2022106313 describes a process for methanol synthesis in presence of CO2that includes an indium oxide catalyst. This document is incorporated by reference.Wherein the second catalytic composition 27 is or comprises an indium oxide catalyst, thetemperature conditions can range between 180°C and 350°C. In a preferred embodiment, thetemperature conditions are at least 270°C; preferably at least 275°C, preferably at least 280°C,more preferably at least 285°C, even more preferably at least 290°C, most preferably at least 280°C, even most preferably at least 290°C, or at least 300°C. For example, temperature conditions are at most 350°C, more preferably at most 340°C. With preference, the temperature conditions range between 270°C and 350°C, more preferably between 280°C and 340°C, and even more preferably between 290°C and 340°C. The temperature conditions are the start-of-run temperature conditions.For example, the catalyst support of the indium oxide catalyst comprises at least one selectedfrom silica (SiO2), alumina (Al2O3), gallium oxide (Ga2O3), cerium oxide (CeO2), vanadium oxide (V2O5), chromium oxide (Cr2O3), zirconium dioxide (ZrO2), titanium dioxide (TiO2), magnesium oxide (MgO), zinc oxide (ZnO), tin oxide (SnO2), carbon black (C), andcombinations thereof. Preferably, the catalyst support of the indium catalyst comprises at leastone selected from zinc oxide (ZnO), zirconium dioxide (ZrO2) and titanium dioxide (TiO2) or acombination thereof; and more preferably the catalyst support of the indium oxide catalyst isor comprises zirconium dioxide. When the catalyst support comprises zirconium dioxide (ZrO2),the zirconium dioxide can be monoclinic, tetragonal, or cubic.The indium oxide catalyst can be a calcined supported catalyst and has preferably a surfacearea (i.e BET surface area) as determined by N2 sorption analysis according to ASTM D3663– 03, in the range of about 5 m2g-1 to about 400 m2 g-1, such as from 30 m2 g-1 to about 200 m2g-1.In a preferred embodiment, the indium oxide catalyst comprises at least one metal as apromoter, wherein preferably both indium oxide and the at least one metal are deposited on a support. With preference, at least one metal is selected from ruthenium (Ru), rhodium (Rh), palladium (Pd), silver (Ag), osmium (Os), platinum (Pt), copper (Cu), nickel (Ni), cobalt (Co),gold (Au), iridium (Ir), and any combinations thereof; preferably a metal selected fromruthenium (Ru), rhodium (Rh), palladium (Pd), silver (Ag), platinum (Pt), copper (Cu), nickel(Ni), cobalt (Co) and any combinations thereof; more preferably, a metal selected fromruthenium (Ru), rhodium (Rh), palladium (Pd), silver (Ag), platinum (Pt), and any combinations thereof; even more preferably, a metal selected from palladium (Pd) and / or platinum (Pt), and most preferably the metal is palladium (Pd).In an embodiment, the indium oxide catalyst is devoid of gold (Au). With preference, said atleast one metal is in an oxidized form.A first methanol-containing stream 29 exits the methanol synthesis unit, such first methanol-containing stream can be recovered.The step e) of separationIn a preferred embodiment, the process further comprises a step e) of separation performedon the first methanol-containing stream 29 to recover a methanol stream 43. The methanol-containing stream 29 is therefore sent to a separation unit 31. In a preferred embodiment, the separation step e) comprises a first sub-step e1) ofcondensation in a condenser 33 (i.e. a low-temperature condenser) that operates at lowtemperatures (e.g., -20 to 50°C) to condense light hydrocarbons and water vapor. The firstsub-step e1) results in a non-condensable gas stream 35 comprising unreacted H2, CO, CO2,and some gaseous C1-C4 hydrocarbons, and a second methanol-containing stream 37 that comprises methanol and water. The second methanol-containing stream 37 can be submitted to a second sub-step e2) ofdistillation to dry and purify it. Distillation can be performed in a distillation column 41. Thesecond sub-step e2) results in a methanol stream 43 and a water stream 45.In a preferred embodiment, the non-condensable gas stream 35 is recycled into thefeedstream 11 provided in step a). Example Plasma catalytic conversionPlasma catalytic conversion was made according to WO 2023 / 037258 A1 using an aluminasupported catalyst wherein the active component comprises a non-noble metal. Theexperiment was conducted at 250°C, 20,000 h-1, at atmosphere pressure.Methanol synthesisData from Aspen: 250°C, 70 bar, equilibrium reactor2 2 (1) (first methanol-containing %mol H +CO Syngas 2) Dried syngas (3)stream(4)CO2 33.3 11.1 14.5 21.9H2 66.7 43.6 56.6 32.4CO - 22.2 28.9 17.8CH3OH - - - 27.4H2O - 23.1 - 0.5(1)Corresponds to reference 13 +15 in Fig.1 (2)Corresponds to reference 21 in Fig.1 (3)Corresponds to reference 25 in Fig.1 (4)Corresponds to reference 29 in Fig.1From the example, it can be seen that the maximum heat demand is 250°C. By contrast, Themaximum heat demand to expect at least similar conversion level with conventional RWGS thermoconversion is >800°C.

Claims

CLAIMS 1. Process to produce methanol from a CO2-containing stream (13), the processcomprising: a) providing a feedstream (11) comprising carbon dioxide and hydrogen, wherein themolar ratio of hydrogen to carbon dioxide in the feedstream ranges from 4:1 to 1:1;b) performing a Reverse Water-Gas Shift (RWGS) reaction on said feedstream (11) toobtain a syngas (21),c) drying the syngas (21) to obtain a dried syngas (25); andd) submitting the dried syngas to a methanol synthesis reaction to obtain a firstmethanol-containing stream (29); wherein the process is characterized in that in step b), the RWGS reaction is performed by plasma catalysis at a temperature below 450°C, wherein the plasma catalysiscomprises generating a plasma in one or more dielectric barrier discharge (DBD)reactors in the presence of a first catalytic composition (19).

2. The process according to claim 1 is characterized in that the first catalytic composition(19) comprises at least an active component wherein the active component comprisesone or more selected from Ni, Fe, Co, Mo, Cu, Au, Ru, Rh, Re, Pd, Ir, Pt, Mn, La, W, Cr, Zn, Y, Zr, Ag, Li, Na, K, Rb, Cs, Mg, Ca, Ce, La, Sc, and Y; with preference, the active component of the first catalytic composition (19) comprises at least one selected from Ni, Fe, Co, Mo, and Cu.

3. The process according to claim 1 or 2 is characterized in that the first catalyticcomposition (19) comprises a catalyst support selected from ZrO2, Al2O3, MgO, SiO2, Al2O3-ZnO, CeO2, TiO2, and any mixture thereof; with preference the catalyst support is or comprises Al2O3 and / or MgO.

4. The process according to any one of claims 1 to 3 is characterized in that the firstcatalytic composition (19) comprises one or more selected from Ni / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Ni / MgO, Ni / SiO₂, Cu / ZnO-Al₂O₃, Cu / SiO₂, Fe / Al₂O₃, Fe / CeO₂, Co / Al₂O₃, Co / SiO₂, CoxOy / MgO, La1-xSrxNiyFeyO3+δ; with preference, selected from Ni / Al₂O₃, Cu / Al₂O₃, Fe-Cu / Al₂O₃, Fe / Al₂O₃, Co / Al₂O₃, CoxOy / MgO, and La1-xSrxNiyFeyO3+δ.

5. The process according to any one of claims 1 to 4 is characterized in that the firstcatalytic composition comprises an active component Fe and at least one metallic compound from Ni, Co, Mo, Cu; with preference, the first catalytic compositioncomprises an active component Fe and at least one metallic compound from Ni, Co,Mo, Cu; and a catalyst support comprising Al2O3and / or MgO.

6. The process according to any one of claims 1 to 5 is characterized in that the RWGSreaction by plasma catalysis is performed at a temperature ranging from 150°C to 300°C; preferably from 200°C to 270°C.

7. The process according to any one of claims 1 to 6 is characterized in that the molarratio of hydrogen to carbon dioxide in the feedstream ranges from 4:1 to 2:1, preferablyfrom 3:1 to 2:1.

8. The process according to any one of claims 1 to 7 is characterized in that the dischargefrequency ranges from 50 to 100 kHz and / or the electrical power supplied ranges from20 to 40 W.

9. The process according to any one of claims 1 to 8 in that step c) drying the syngas isperformed by sorbents, membrane separation, condensation, cryogenic distillation, or any combination thereof.

10. The process according to any one of claims 1 to 9 is characterized in that the dryingstep further includes a sub-step of adjusting the hydrogen content of the syngas (21) and / or of the dried syngas (25) to obtain a hydrogen-to-carbon monoxide molar ratio of at least 2:1.

11. The process according to any one of claims 1 to 10 is characterized in that the dryingstep comprises a step of CO2 removal; preferably the step of CO2 removal is performed by condensation or by cryogenic distillation.

12. The process according to any one of claims 1 to 11 is characterized in that each of theRWGS reaction and the methanol synthesis reaction are performed at a temperatureof at most 350°C; with preference at most 300°C; more preferably at most 280°C.

13. The process according to any one of claims 1 to 12 is characterized in that the methanolsynthesis is performed at a temperature ranging from 180 to 350°C, using a second catalytic composition (27) that is or comprises one or more selected from a copper zincoxide catalyst, an indium oxide catalyst, Cu-ZnO / Al2O3, Cu-ZnO-Ga2O3 / SiO2, Cu-ZnO-Al2O3 / ZrO2, ZnO, Au / ZnO, Au / Fe2O3, Au / TiO2, Au / ZrO2, Au / La2O3, Au / ZnFe2O4, Fe2O3,Au / Fe2O3, Cu / ZnO, CeO2, TiO2, ZrO2, La2O3, Zn / Fe2O3, and a combination thereof;preferably at a pressure ranging between 5.0 and 10.0 MPa.

14. The process according to any one of claims 1 to 13 is characterized in that the processfurther comprises a step e) of separation of the first methanol-containing stream (29)comprising first sub-step e1) of condensation resulting in a non-condensable gasstream (35) and a second methanol-containing stream (37).

15. The process according to claim 14 is characterized in that the process furthercomprises recycling the non-condensable gas stream (35) into the feedstream (11)provided in step a).

16. The process according to claim 14 or 15 is characterized in that the step e) ofseparation of the first methanol-containing stream (29) comprises a second sub-step e2) of distillation that is performed on the second methanol-containing stream (37) to obtain methanol stream (43).

17. Installation (1) to carry out the process according to any one of the preceding claimscharacterized in that it comprises, in the following order: -an RWGS unit (3) comprising at least one plasma catalytic reactor;- a drying unit (7); and- a methanol synthesis unit (9) comprising one or more reactors;with preference, the installation further comprises a CO2-H2 blending zone (17) and / ora separation unit (31).

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