Transformative methanol production by sustainable hydrogen integration balanced by co 2

Abstract

The present invention relates to a process for preparing methanol, the process comprising pre-paring a make-up gas stream comprising CO and H2, a CO2-containing gas stream, and a H2- containing gas stream; combining of said streams, obtaining a reaction gas stream, wherein the reaction gas stream displays an S value of greater than 1.95; and feeding the reaction gas stream into a reactor comprising a catalyst, and contacting the reaction gas stream with the catalyst, obtaining a product gas stream comprising CH3OH. In particular, it has been surprisingly found that a hydrogen supply can be integrated in an existing methanol process, if a CO2-containing gas stream is further added within certain boundaries to generate a suitable reaction gas stream for preparing methanol.

Description

Transformative methanol production by sustainable hydrogen integration balanced byCO2TECHNICAL FIELDThe present invention relates to a process for preparing methanol (CH3OH), wherein in addition to a make-up gas stream comprising H2, CO2 and CO, a ^-containing gas stream and a CO2- containing gas stream are used. In said methanol process sustainable hydrogen can be integrated in the ^-containing gas stream. The additional hydrogen from the ^-containing stream has to be balanced with CO2. Thus, a transformative methanol production concept can be provided enabling, besides the conventionally produced methanol, an additional low product carbon foot print (PCF) methanol as part of a dynamic regenerative energy production within a carbon capture and utilization (CCU) concept.INTRODUCTIONIndustrially, methanol is produced from a syngas mixture mainly comprising CO, CO2 and H2. The reaction follows equations (1)-(3) and is conducted at elevated pressures of 30 to 100 bara and temperatures between 190 and 300 °C. This refers to a so-called low-pressure methanol process, which is described in “Ullmann's Encyclopedia of Industrial Chemistry, Chapter-Metha- nol, 2012 Wiley-VCH”.CO + 2H2CH3OH (1).CO2+ 3H2CH3OH + H2O (2).CO2+ H2CO + H2O (3).The syngas or make-up gas (MUG) of the methanol process has to fulfill certain stoichiometric requirements for methanol formation. The so-called stoichiometric number S, calculated as S = (n(H2)-n(CO2)) / (n(CO) + n(CO2)), is an important value therefor and has to be higher than 2, whereby a value of 1 .95 can sometimes be enough to have a suitable stoichiometric value in the process, especially for cases wherein CO2loss as flash gas in gas-liquid-separators occurs.US 11292717 B2 relates to a process for preparing methanol from a carbon-containing feedstock by producing synthesis gas therefrom in a synthesis gas production unit, converting the synthesis gas to methanol in a methanol synthesis unit and working up the reaction mixture to isolate the methanol, wherein the carbon monoxide, carbon dioxide, dimethyl ether and methane components of value from the streams separated off in the isolation of the methanol are combusted with an oxygenous gas, and the carbon dioxide in the resultant flue gas is separated off in a carbon dioxide recovery unit and recycled to the synthesis gas production unit and / or to the methanol synthesis unit.US 2024 / 059637 A1 relates to a process and a plant for producing carbon dioxide-based methanol and synthesis gas, wherein the produced synthesis gas may be utilized process-internally for methanol synthesis.There is an ongoing interest of replacing conventional hydrogen sources by comparatively more sustainable hydrogen sources, as for example electrolysis of water using green energy. However, since supply of green energy typically fluctuates, also the available amount of hydrogen fluctuates similarly. Especially, the electrolysis of water by regenerative power is a non-static process, where the hydrogen supply constantly fluctuates.Thus, there was a need to provide a process for preparing methanol, in particular as a downstream application of the production of sustainable hydrogen, allowing to adapt to this dynamic behavior.DETAILED DESCRIPTIONSurprisingly, it has been found that by combining a make-up gas stream (or syngas stream), a CO2-containing stream and a ^-containing stream, a reaction gas stream can be provided suitable for preparing methanol, if the reaction gas stream fulfills certain conditions. In particular, it has surprisingly been found that a hydrogen supply can be integrated in an existing methanol process, if a CO2-containing gas stream is further added within certain boundaries to generate a suitable reaction gas stream for preparing methanol.Thus, it has surprisingly been found that with this transformative methanol production concept, not only the hydrogen fluctuations can be smoothly integrated, but also the production capacity of an existing methanol plant can be increased. Furthermore, it has surprisingly been found that the additionally produced methanol has a significantly lower PCF as part of a CCU concept.Therefore, the present invention relates to a process for preparing methanol, the process comprising(i) preparing a make-up gas stream comprising CO and H2;(ii) preparing a CO2-containing gas stream;(iii) preparing a ^-containing gas stream;(iv) combining the make-up gas stream prepared in (i), the CO2-containing gas stream prepared in (ii), and the ^-containing gas stream prepared in (iii), obtaining a reaction gas stream, wherein the reaction gas stream obtained from (iv) displays an S value of greater than 1 .95, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2)) I (n(CO) + n(CO2)) (I);(v) feeding the reaction gas stream obtained from (iv) into a reactor comprising a catalyst, and contacting the reaction gas stream with the catalyst, obtaining a product gas stream comprising CH3OH.It is preferred that the make-up gas stream further comprises CO2, wherein the make-up gas stream prepared in (i) preferably comprises less than 10 volume-%, more preferably less than 7 volume-%, more preferably less than 5 volume-%, more preferably less than 3 volume-%, of CO2.In the case wherein the make-up gas stream further comprises CO2, it is preferred that the H2:CC>2 molar ratio in the make-up gas stream prepared in (i) is in the range of from 1 :1 to 40:1 , preferably from 2:1 to 27:1 , more preferably from 3:1 to 23:1 , more preferably from 5:1 to 20:1 , more preferably from 10:1 to 15:1.Further in the case wherein the make-up gas stream further comprises CO2, it is preferred that the CO:CC>2 molar ratio in the make-up gas stream prepared in (i) is in the range of from 0.1 :1 to 30:1 , more preferably from 0.5:1 to 25:1 , more preferably from 1 :1 to 20:1 , more preferably from 2:1 to 15:1 , more preferably from 5:1 to 10:1.It is preferred that the make-up gas stream prepared in (i) comprises from 50 to 80 volume-%, more preferably from 53 to 78 volume-%, more preferably from 55 to 76 volume-%, of H2.It is preferred that the make-up gas stream prepared in (i) comprises from 1 to 40 volume-%, more preferably from 2 to 37 volume-%, more preferably from 3 to 35 volume-%, of CO.It is preferred that the H2:CO molar ratio in the make-up gas stream prepared in (i) is in the range of from 0.1 :1 to 100:1 , more preferably from 0.5:1 to 50:1 , more preferably from 1 :1 to 10:1 , more preferably from 1.5:1 to 4:1 , more preferably from 2:1 to 3:1.It is preferred that the make-up gas stream prepared in (i) is obtainable or obtained by a process comprising one or more of acetylene production, a gasification, steam reforming, and autothermal reforming of one or more of natural gas and biogas.It is preferred that from 50 to 100 volume-%, more preferably from 90 to 100 volume-%, more preferably from 90 to 100 volume-%, more preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the CCh-containing gas stream prepared in (ii) consists of CO2.It is preferred that the CCh-containing gas stream prepared in (ii) is obtainable or obtained from a chemical production plant, more preferably from a power plant, a steam cracker, an ethylene oxide production plant, an acetylene production plant, or an ammonia plant.It is preferred that the CCh-containing gas stream prepared in (ii) has a volume flow rate in the range of from 5,000 to 300,000 Nm3 / h, more preferably from 10,000 to 100,000 Nm3 / h, more preferably from 15,000 to 25,000 Nm3 / h.It is preferred that from 50 to 100 volume-%, more preferably from 90 to 100 volume-%, more preferably from 90 to 100 volume-%, more preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the ^-containing gas stream prepared in (iii) consists of H2.It is preferred that the ^-containing gas stream prepared in (iii) is obtainable or obtained by a process comprising one or more of water electrolysis, green NH3 reforming, bio-methane reforming, propane dehydrogenation, and iso-butane dehydrogenation.It is preferred that the ^-containing gas stream prepared in (iii) has a volume flow rate in the range of from 100 to 900,000 Nm3 / h, more preferably from 5,000 to 25,000 Nm3 / h, more preferably from 15,000 to 21 ,000 Nm3 / h.It is preferred that the reaction gas stream obtained from (iv) comprises from 50 to 85 volume- %, more preferably from 62 to 72 volume-%, more preferably from 66 to 68 volume-%, of H2.It is preferred that the reaction gas stream obtained from (iv) comprises from 2 to 30 volume-%, more preferably from 10 to 28 volume-%, more preferably from 19 to 26 volume-%, more preferably from 21 to 24 volume-%, of CO.It is preferred that the reaction gas stream obtained from (iv) comprises from 3 to 26 volume-%, more preferably from 4 to 15 volume-%, more preferably from 5 to 9 volume-%, more preferably from 6 to 8 volume-%, of CO2.It is preferred that the H2:CO2 molar ratio in the reaction gas stream obtained from (iv) is in the range of from 3:1 to 20.0:1 , more preferably from 8.0:1 to 18.0:1 , more preferably from 8.6:1 to 17.0:1 , more preferably from 8.8:1 to 15.0:1 , more preferably from 9.0:1 to 13.0:1 , more preferably from 9.2:1 to 11.0:1 , more preferably from 9.4:1 to 10.5:1 , more preferably from 9.5:1 to 10.1 :1.It is preferred that the H2:CO molar ratio in the reaction gas stream obtained from (iv) is in the range of from 1.0:1 to 5.0:1 , more preferably from 2.0:1 to 4.0:1 , more preferably from 2.5:1 to 3.5:1 , more preferably from 2.8:1 to 3.1 :1 , more preferably from 2.9:1 to 3.0:1.It is preferred that the CO:CC>2 molar ratio in the reaction gas stream obtained from (iv) is in the range of from 0.1 :1 to 9.1 :1 , more preferably from 1.0:1 to 7.5:1 , more preferably from 2.0:1 to 6.0:1 , more preferably from 3.0:1 to 4.0:1 , more preferably from 3.1 :1 to 3.6:1 , more preferably from 3.2:1 to 3.4:1.It is preferred that the reaction gas stream obtained from (iv) displays a S value of greater than 1.95, more preferably in the range of from 2.00 to 2.10, more preferably from 2.01 to 2.06, more preferably from 2.02 to 2.04, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2)) I (n(CO) + n(CO2)) (I).It is preferred that the reaction gas stream obtained from (iv) has a volume flow rate in the range of from 10,000 to 1000,000 Nm3 / h, more preferably from 50,000 to 200,000 Nm3 / h, more preferably from 100,000 to 130,000 Nm3 / h.It is preferred that the catalyst comprised in the reactor according to (v) comprises one or more of Cu, Zn, Al, Zr, Si, and O, more preferably Cu, Zn, Al, Zr, Si, and O.It is preferred that the catalyst comprised in the reactor according to (v) comprises elemental copper.It is preferred that the catalyst comprised in the reactor according to (v) displays a Zn : Si atomic ratio in the range of from 5:1 to 27:1 , more preferably of from 5.5:1 to 25:1 , more preferably of from 6:1 to 20:1 , more preferably of from 6.5:1 to 15:1 , more preferably of from 7:1 to 12:1 , more preferably of from 7.5:1 to 10:1 , more preferably of from 8:1 to 9:1.It is preferred that the catalyst comprised in the reactor according to (v) comprises one or more oxides of Zn, Al, Zr, and Si, wherein the catalyst more preferably comprises one or more oxides selected from the group consisting of ZnO, ZnAhCU, and CUAI2O4, wherein more preferably the catalyst comprises ZnO and ZnAhO4, or ZnO and CUAI2O4, or ZnO, ZnAhO4, and CUAI2O4.It is preferred that the catalyst comprised in the reactor according to (v) displays a BET surface area of 130 m2 / g or less, and more preferably displays a BET surface area within the range of from 60 to 130 m2 / g, wherein the BET surface area is more preferably determined according to Reference Example 1.It is preferred that the catalyst comprised in the reactor according to (v) displays a copper surface area in the range of from 5 to 15 m2 / g, more preferably for from 10 to 13 m2 / g, wherein the copper surface area is preferably determined according to Reference Example 2.It is preferred that the catalyst comprised in the reactor according to (v) comprises SiC>2.It is preferred that the catalyst comprised in the reactor according to (v) displays Cu : Zn : Al : Zr : Si molar ratios in the ranges of (40 - 65) : (10 - 25) : (15 - 40) : (0.2 - 10) : (0.1 - 5), more preferably of (45 - 62) : (13 - 23) : (18 - 35) : (0.5. - 5) : (0.3 - 4.5), more preferably of (50 - 59) : (15 - 21) : (22 - 30) : (1 - 4) : (0.8 - 4), and more preferably of (55 - 56) : (17 - 19) : (25 - 26) : (1.4 - 3) : (1.2 - 3.6).It is preferred that from 95 to 100 weight-% of the catalyst comprised in the reactor according to (v) consists of Cu, Zn, Al, Zr, Si, and O, more preferably from 97 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%.It is preferred that contacting according to (v) is performed at a temperature in the range of from 190 to 350 °C, more preferably from 230 to 260 °C.It is preferred that contacting according to (v) is performed at a pressure in the range of from 1 to 100 bara, more preferably in the range of from 40 to 85 bara, more preferably from 70 to 82 bara, and more preferably from 74 to 81 bara.It is preferred that the product gas stream comprises CO2, wherein the product gas stream comprises from 0.1 to 25 volume-%, more preferably from 0.5 to 23 volume-%, more preferably from 1 to 22 volume-%, of CO2.It is preferred that the product gas stream comprises H2, wherein the product gas stream comprises from 50 to 90 volume-%, more preferably from 53 to 87 volume-%, more preferably from 55 to 85 volume-%, of H2.It is preferred that the product gas stream comprises one or more of CO2 and H2, preferably CO2 and H2.In the case wherein the product gas stream comprises one or more of CO2 and H2, it is preferred that the process further comprises(vi) separating the product stream into a CHsOH-containing stream, wherein the CHsOH-con- taining stream is preferably liquid, and a recycle stream comprising one or more of CO2 and H2, preferably CO2 and H2, wherein the recycle stream is preferably gaseous. In the case wherein the process comprises separating the product stream into a CHsOH-contain- ing stream and a recycle stream comprising one or more of CO2 and H2 according to (vi), it is preferred that at least a portion of the recycle stream is recycled into the make-up gas stream prepared in (i).According to a further aspect, the present invention relates to a process, preferably to the process as described above, which (further) comprises the step of converting the methanol obtainable by or obtained by the process described herein to obtain a product Q. Yet further, the present invention relates to a process comprising the step of using the methanol obtainable by or obtained by the process described herein and converting the methanol to obtain a product Q.Yet further, the present invention relates to a product Q, preferably a product Q according to any one of the embodiments described herein, obtained or obtainable by a process using methanol,in particular using methanol obtained from the process according to any one of the embodiments disclosed herein and converting the methanol to obtain a product Q.Preferably, the product Q is selected from: building block or monomer; or polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acry- late hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.Regarding this process from which the product Q is obtained, it is preferred: that the content of C stemming from the methanol obtained from the process according to any one of the embodiments disclosed herein, wherein C is calculated as the element, in the product Q, is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or that the content of C stemming from the methanol obtained from the process according to any one of the embodiments disclosed herein, wherein C is calculated as the element, in the product Q is 100 weight-% or less, preferably 95 weight-% or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less;wherein it is more preferred that the respective content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety. Preferably, the product Q is a product as described in Reference RF1 ; paragraphs

[1000] to

[8005] , Preferably, the process described herein is further a process for the production of a product.The converting step to obtain the product Q preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and / or steam cracking; and / or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, preferably coating and / or smoothing.In addition, the one or more step(s) are described in detail in Reference RF1 ; paragraphs

[1000] to

[8005] ,The term “building block”, as used in the context of the product Q herein, comprises compounds, which are in a gaseous, liquid or solid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and / or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxid, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.The term “monomer”, as used in the context of the product Q herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acrylic acid; inparticular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Methacrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term “intermediate compound”, as used in the context of the product Q herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI).The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs

[1000] to

[1012] of Reference RF1.The term “polymer A”, as used in the context of the product Q herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1.The term “polymer composition A”, as used in the context of the product Q herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and / or flame retardant, and is defined in more detail in paragraph

[2008] of Reference RF1.The term “polymer product A”, as used in the context of the product Q herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is defined in more detail in paragraphs

[2009] and

[2010] of Reference RF1.The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymer composition A or polymer product, preferably polymer product A is / are described in more detail in paragraph

[2011] of Reference RF1.The term “industrial use polymer”, as used in the context of the product Q herein, comprises rheology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, poly- ether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term “industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use sur-factants defined in more detail in paragraphs

[3008] to

[3034] of Reference RF1. The term “industrial use descaling compound”, as used in the context of the product Q herein, comprises non-phosphate based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs

[3001] to

[3005] of Reference RF1. The term “industrial use biocide”, as used in the context of the product Q herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs

[3006] to

[3007] of Reference RF1. The term “industrial use solvent”, as used in the context of the product Q herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1. The term “industrial use dispersant”, as used in the context of the product Q herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs

[3056] to

[3058] of Reference RF1. The term “composition and / or formulation thereof” with reference to the industrial use polymers, industrial use surfactants, descaling compounds and / or industrial use biocides refers to industrial use compositions and / or institutional use products and / or fabric and home care products and / or personal care products defined in more detail in paragraph

[3059] of Reference RF1. The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3060] of Reference RF1. The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3061] of Reference RF1.The term “agrochemical composition”, as used in the context of the product Q herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1 , paragraph

[4001] ,The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer” and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof” may beperformed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used in the context of the product Q herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used in the context of the product Q herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph

[5001] of Reference RF1.The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used in the context of the product Q herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2-propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole / polyvinylpyrrolidone-co- polymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

[5002] of Reference RF1.The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms aroma chemical and aroma composition as used in the context of the product Q herein, comprise a volatile organic substance with a molecular weight between 70-250 g / mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more detail in paragraph

[5003] of Reference RF1.The converting step(s) to obtain the aroma chemical and aroma composition may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term “aqueous polymer dispersion”, as used in the context of the product Q herein, comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled “aqueous polymer dispersion” of Reference RF1. The dispersed polymers) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term “emulsion polymer”, as used in the context of the product Q herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section

[6002] entitled “Polyurethane dispersions” of Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

[6017] of Reference RF1. Polyurethane - poly(meth) acrylate hybrid polymer(s) is / are defined in more detail in the section

[6016] of Reference RF1.The term “polymeric dispersant”, as used in the context of the product Q herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph

[6020] entitled “Polymeric dispersant” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is / are defined in more detail in the section

[6003] entitled “Emulsion polymerization” of Reference RF1.The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is / are defined in more detail in the section

[6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section [6017)] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1. Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section

[6004] entitled “Uses of aqueous polymer dispersions”, section

[6005] entitled “Binders for architectural and construction coatings” section

[6006] entitled “Binders for paper coating” section

[6007] entitled “Binders for fiber bonding” section

[6008] entitled “Adhesive polymers and adhesive compositions” section

[6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions” section

[6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions” section

[6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” section

[6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use”

[6019] 100% curable coating compositionsUV-crosslinkable poly(meth)acrylate(s) and its / their uses are defined in more detail in section

[6009] entitled “UV-crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hotmelt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1.Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

[6010] entitled “Polyisocyanates” of Reference RF1.Hyperbranched polyester polyol(s) and its / their uses are defined in more detail in section

[6011] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1. The converting step(s) to obtain the hyperbranched polyester polyols is / are defined in more detail in the section

[6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1. Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

[6013] entitled “Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1.Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section

[6018] entitled “Organic solvent based coating composition comprising unsaturated polyester polyols” of Reference RF1. 100% curable coating composition(s) is / are defined in more detail in section

[6019] of Reference RF1.Polymeric dispersant(s) for inorganic binder compositions is / are defined in more detail in section

[6020] of Reference RF1. The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section

[6021] of Reference RF1. The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section

[6020] of Reference RF1. The term “inorganic binder composition” comprising the polymeric dispersants), as used in the context of the product Q herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section

[6021] of Reference RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section

[6021] of Reference RF1.The term “cosmetic surfactant”, as used in the context of the product Q herein, comprises nonionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph

[7002] of Reference RF1. The term “emollient”, as used in the context of the product Q herein, refers to a chemical compound used for protecting, moisturizing, and / or lubricating the skin and is defined in more detail in paragraph

[7003] of Reference RF1. The term “wax”, as used in the context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

[7004] of Reference RF1. The term “cosmetic polymer”, as used in the context of the product Q herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1. The term “UV filter”, as used in the context of the product Q herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph

[7006] of Reference RF1. The term “further cosmetic ingredient”, as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients. The term “composition and / or formulation thereof” with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredientrefers to personal care and / or cosmetic compositions or formulations defined in more detail in paragraph

[7007] of Reference RF1. The converting step(s) to obtain the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is / are defined in more detail in paragraph

[7008] of Reference RF1.The terms “polymer B”, “polymer composition B”, “coating composition”, “other functional composition”, “foil”, “molded body”, “coating” and “coated substrate” are well known to the person skilled in the art and are defined in more detail from paragraph

[8000] to

[8005] of Reference RF1.In the context of the present invention, indication of Nm3relates to a volume in cubic meter at standard conditions, in particular at a pressure of 1013.25 mbara and a temperature of 15 °C, in accordance with ISO 2533.The unit bara refers to an absolute pressure wherein 1 bar equals 105Pa.The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1 , 2, 3 and 4". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.1 . A process for preparing methanol, the process comprising(i) preparing a make-up gas stream comprising CO and H2;(ii) preparing a CO2-containing gas stream;(iii) preparing a H2-containing gas stream;(iv) combining the make-up gas stream prepared in (i), the CO2-containing gas stream prepared in (ii), and the H2-containing gas stream prepared in (iii), obtaining a reaction gas stream, wherein the reaction gas stream obtained from (iv) displays an S value of greater than 1.95, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2)) I (n(CO) + n(CO2)) (I);(v) feeding the reaction gas stream obtained from (iv) into a reactor comprising a catalyst, and contacting the reaction gas stream with the catalyst, obtaining a product gas stream comprising CH3OH.2. The process of embodiment 1 , wherein the make-up gas stream further comprises CO2, wherein the make-up gas stream prepared in (i) preferably comprises less than 10 vol- ume-%, more preferably less than 7 volume-%, more preferably less than 5 volume-%, more preferably less than 3 volume-%, of CO2.3. The process of embodiment 2, wherein the H2:CO2molar ratio in the make-up gas stream prepared in (i) is in the range of from 1 :1 to 40:1 , preferably from 2:1 to 27:1 , more preferably from 3:1 to 23:1 , more preferably from 5:1 to 20:1 , more preferably from 10:1 to 15:1.4. The process of embodiment 2 or 3, wherein the CO:CO2molar ratio in the make-up gas stream prepared in (i) is in the range of from 0.1 :1 to 30:1 , preferably from 0.5:1 to 25:1 , more preferably from 1 :1 to 20:1 , more preferably from 2:1 to 15:1 , more preferably from 5:1 to 10:1.5. The process of any one of embodiments 1 to 4, wherein the make-up gas stream prepared in (i) comprises from 50 to 80 volume-%, preferably from 53 to 78 volume-%, more preferably from 55 to 76 volume-%, of H2.6. The process of any one of embodiments 1 to 5, wherein the make-up gas stream prepared in (i) comprises from 1 to 40 volume-%, preferably from 2 to 37 volume-%, more preferably from 3 to 35 volume-%, of CO.7. The process of any one of embodiments 1 to 6, wherein the H2:CO molar ratio in the make-up gas stream prepared in (i) is in the range of from 0.1 :1 to 100:1 , preferably from 0.5:1 to 50:1 , more preferably from 1 :1 to 10:1 , more preferably from 1.5:1 to 4:1 , more preferably from 2:1 to 3:1.8. The process of any one of embodiments 1 to 7, wherein the make-up gas stream prepared in (i) is obtainable or obtained by a process comprising one or more of acetylene production, a gasification, steam reforming, and autothermal reforming of one or more of natural gas and biogas.The process of any one of embodiments 1 to 8, wherein from 50 to 100 volume-%, preferably from 90 to 100 volume-%, more preferably from 90 to 100 volume-%, more preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the CO2-containing gas stream prepared in (ii) consists of CO2. The process of any one of embodiments 1 to 9, wherein the CO2-containing gas stream prepared in (ii) is obtainable or obtained from a chemical production plant, preferably from a power plant, a steam cracker, an ethylene oxide production plant, an acetylene production plant, or an ammonia plant. The process of any one of embodiments 1 to 10, wherein the CO2-containing gas stream prepared in (ii) has a volume flow rate in the range of from 5,000 to 300,000 Nm3 / h, preferably from 10,000 to 100,000 Nm3 / h, more preferably from 15,000 to 25,000 Nm3 / h. The process of any one of embodiments 1 to 11 , wherein from 50 to 100 volume-%, preferably from 90 to 100 volume-%, more preferably from 90 to 100 volume-%, more preferably from 95 to 100 volume-%, more preferably from 99 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the (^-containing gas stream prepared in (iii) consists of H2. The process of any one of embodiments 1 to 12, wherein the (^-containing gas stream prepared in (iii) is obtainable or obtained by a process comprising one or more of water electrolysis, green NH3 reforming, propane dehydrogenation, and iso-butane dehydrogenation. The process of any one of embodiments 1 to 13, wherein the (^-containing gas stream prepared in (iii) has a volume flow rate in the range of from 100 to 900,000 Nm3 / h, preferably from 5,000 to 25,000 Nm3 / h, more preferably from 15,000 to 21 ,000 Nm3 / h. The process of any one of embodiments 1 to 14, wherein the reaction gas stream obtained from (iv) comprises from 50 to 85 volume-%, preferably from 62 to 72 volume-%, more preferably from 66 to 68 volume-%, of H2.16. The process of any one of embodiments 1 to 15, wherein the reaction gas stream obtained from (iv) comprises from 2 to 30 volume-%, preferably from 10 to 28 volume-%, more preferably from 19 to 26 volume-%, more preferably from 21 to 24 volume-%, of CO.17. The process of any one of embodiments 1 to 16, wherein the reaction gas stream obtained from (iv) comprises from 3 to 26 volume-%, preferably from 4 to 15 volume-%, more preferably from 5 to 9 volume-%, more preferably from 6 to 8 volume-%, of CO2.18. The process of any one of embodiments 1 to 17, wherein the H2:CO2 molar ratio in the reaction gas stream obtained from (iv) is in the range of from 3:1 to 20.0:1 , preferably from 8.0:1 to 18.0:1 , more preferably from 8.6:1 to 17.0:1 , more preferably from 8.8:1 to 15.0:1 , more preferably from 9.0:1 to 13.0:1 , more preferably from 9.2:1 to 11.0:1 , more preferably from 9.4:1 to 10.5:1 , more preferably from 9.5:1 to 10.1 :1.19. The process of any one of embodiments 1 to 18, wherein the H2:CO molar ratio in the reaction gas stream obtained from (iv) is in the range of from 1.0:1 to 5.0:1 , preferably from 2.0:1 to 4.0:1 , more preferably from 2.5:1 to 3.5:1 , more preferably from 2.8:1 to 3.1 :1 , more preferably from 2.9:1 to 3.0:1.20. The process of any one of embodiments 1 to 19, wherein the CO:CC>2 molar ratio in the reaction gas stream obtained from (iv) is in the range of from 0.1 :1 to 9.1 :1 , preferably from 1.0:1 to 7.5:1 , more preferably from 2.0:1 to 6.0:1 , more preferably from 3.0:1 to 4.0:1 , more preferably from 3.1 :1 to 3.6: 1 , more preferably from 3.2:1 to 3.4: 1.21 . The process of any one of embodiments 1 to 20, wherein the reaction gas stream obtained from (iv) displays a S value of greater than 1.95, preferably in the range of from 2.00 to 2.10, more preferably from 2.01 to 2.06, more preferably from 2.02 to 2.04, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2)) I (n(CO) + n(CO2)) (I).22. The process of any one of embodiments 1 to 21 , wherein the reaction gas stream obtained from (iv) has a volume flow rate in the range of from 10,000 to 250,000 Nm3 / h, preferably from 50,000 to 200,000 Nm3 / h, more preferably from 100,000 to 130,000 Nm3 / h.23. The process of any one of embodiments 1 to 22, wherein the catalyst comprised in the reactor according to (v) comprises one or more of Cu, Zn, Al, Zr, Si, and O, preferably Cu, Zn, Al, Zr, Si, and O.24. The process of any one of embodiments 1 to 23, wherein the catalyst comprised in the reactor according to (v) comprises elemental copper.25. The process of any one of embodiments 1 to 24, wherein the catalyst comprised in the reactor according to (v) displays a Zn : Si atomic ratio in the range of from 5:1 to 27:1 , preferably of from 5.5:1 to 25:1 , more preferably of from 6:1 to 20:1 , more preferably of from 6.5:1 to 15:1 , more preferably of from 7:1 to 12:1 , more preferably of from 7.5:1 to 10:1 , more preferably of from 8:1 to 9:1.26. The process of any one of embodiments 1 to 25, wherein the catalyst comprised in the reactor according to (v) comprises one or more oxides of Zn, Al, Zr, and Si, wherein the catalyst preferably comprises one or more oxides selected from the group consisting of ZnO, ZnAhOt, and CUAI2O4, wherein more preferably the catalyst comprises ZnO and ZnAhO4, or ZnO and CUAI2O4, or ZnO, ZnAhO4, and CUAI2O4.27. The process of any one of embodiments 1 to 26, wherein the catalyst comprised in the reactor according to (v) displays a BET surface area of 130 m2 / g or less, and preferably displays a BET surface area within the range of from 60 to 130 m2 / g, wherein the BET surface area is preferably determined according to Reference Example 1 .28. The process of any one of embodiments 1 to 27, wherein the catalyst comprised in the reactor according to (v) displays a copper surface area in the range of from 5 to 15 m2 / g, preferably for from 10 to 13 m2 / g, wherein the copper surface area is preferably determined according to Reference Example 2.29. The process of any one of embodiments 1 to 28, wherein the catalyst comprised in the reactor according to (v) comprises SiC>2.30. The process of any one of embodiments 1 to 29, wherein the catalyst comprised in the reactor according to (v) displays Cu : Zn : Al : Zr : Si molar ratios in the ranges of (40 - 65) : (10 - 25) : (15 - 40) : (0.2 - 10) : (0.1 - 5), preferably of (45 - 62) : (13 - 23) : (18 - 35) : (0.5. - 5) : (0.3 - 4.5), more preferably of (50 - 59) : (15 - 21) : (22 - 30) : (1 - 4) : (0.8 - 4), and more preferably of (55 - 56) : (17 - 19) : (25 - 26) : (1.4 - 3) : (1.2 - 3.6).31 . The process of any one of embodiments 1 to 30, wherein from 95 to 100 weight-% of the catalyst comprised in the reactor according to (v) consists of Cu, Zn, Al, Zr, Si, and O, preferably from 97 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, more preferably from 99.9 to 100 weight-%.32. The process of any one of embodiments 1 to 31 , wherein contacting according to (v) is performed at a temperature in the range of from 190 to 350 °C, preferably from 230 to 260 °C.33. The process of any one of embodiments 1 to 32, wherein contacting according to (v) is performed at a pressure in the range of from 1 to 100 bara, preferably in the range of from 40 to 85 bara, more preferably from 70 to 82 bara, and more preferably from 74 to 81 bara.34. The process of any one of embodiments 1 to 33, wherein the product gas stream comprises CO2, wherein the product gas stream comprises from 0.1 to 25 volume-%, preferably from 0.5 to 23 volume-%, more preferably from 1 to 22 volume-%, of CO2.35. The process of any one of embodiments 1 to 34, wherein the product gas stream comprises H2, wherein the product gas stream comprises from 50 to 90 volume-%, preferably from 53 to 87 volume-%, more preferably from 55 to 85 volume-%, of H2.36. The process of any one of embodiments 1 to 35, wherein the product gas stream comprises one or more of CO2 and H2, preferably CO2 and H2.37. The process of embodiment 36, the process further comprising(vi) separating the product stream into a CHsOH-containing stream, wherein the CHsOH-containing stream is preferably liquid, and a recycle stream comprising one or more of CO2 and H2, preferably CO2 and H2, wherein the recycle stream is preferably gaseous.38. The process of embodiment 37, wherein at least a portion of the recycle stream is recycled into the make-up gas stream prepared in (i).39. A process, preferably the process according to any one of embodiments 1 to 38, comprising a step of converting the methanol obtainable or obtained by the process according to any one of embodiments 1 to 38 to obtain a product Q.The present invention is further illustrated by the following examples and comparative examples.EXPERIMENTAL SECTIONReference Example 1 : Determination of BET surface areaThe BET specific surface area was determined via nitrogen physisorption at 77 K according to the method disclosed in DIN 66131.Reference Example 2: Determination of Cu surface areaThe Cu surface area was determined according to the method disclosed in EP 0202824 A using N2O and the pulse method at 25 °C.Comparative Example 3 and Example 4: Process for preparing methanolFor Comparative Example 3 a syngas stream, a FL-containing gas stream obtained from pressure swing adsorption, and an additional FL-containing gas stream were provided having the compositions shown in Table 1 below. By combining said streams, a make-up gas stream was prepared having the composition shown in Table 1 below.For Example 4 a syngas stream, a CCh-containing gas stream, a FL-containing gas stream obtained from pressure swing adsorption, and an additional FL-containing gas stream obtained from regenerative sources were provided having the compositions shown in Table 1 below. By combining said streams, a make-up gas stream was prepared having the composition shown in Table 1 below.Table 1Sources and compositions of gas streams used for Comparative Example 3 and Example 4.For each of the examples, a reactor was provided comprising a Cu-containing catalyst. First, the catalyst was activated in a reductive atmosphere (5 % H2 in Ar) and a temperature of up to 250 °C.Once the activation was completed, the respective make-up gas was fed into the reactor at a gas hourly space velocity (GHSV) in the range of from 6000 to 12000 h-1and at a pressure of 80 bara. For Comparative Example 3, a product gas stream was obtained yielding 38674 kg / h of methanol, and for Example 4 a product gas stream was obtained yielding 44645 kg / h of methanol.DESCRIPTION OF FIGURESFigure 1 : schematically shows the process in accordance with the present invention, wherein in particular A relates to a source for green H2, B to a source for CO2 from a com- bustion or a chemical process, C to a source for syngas, D to a source for H2 from a chemical site, and E to a MeOH comprising product having a low PCF.CITED LITERATURE - US 11292717 B2Ullmann’s Encyclopedia of Industrial Chemistry 2012, Chapter Methanol- US 2024 / 059637 A1

Claims

1. Claims1. A process for preparing methanol, the process comprising(i) preparing a make-up gas stream comprising CO and H2;(ii) preparing a CO2-containing gas stream;(iii) preparing a ^-containing gas stream;(iv) combining the make-up gas stream prepared in (i), the CO2-containing gas stream prepared in (ii), and the ^-containing gas stream prepared in (iii), obtaining a reaction gas stream, wherein the reaction gas stream obtained from (iv) displays an S value of greater than 1.95, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2)) I (n(CO) + n(CO2)) (I);(v) feeding the reaction gas stream obtained from (iv) into a reactor comprising a catalyst, and contacting the reaction gas stream with the catalyst, obtaining a product gas stream comprising CH3OH.

2. The process of claim 1, wherein the make-up gas stream prepared in (i) is obtainable or obtained by a process comprising one or more of acetylene production, a gasification, steam reforming, and autothermal reforming of one or more of natural gas and biogas.

3. The process of claim 1 or 2, wherein the make-up gas stream further comprises CO2.

4. The process of claim 3, wherein the make-up gas stream prepared in (i) comprises less than 10 volume-% of CO2.

5. The process of claim 4, wherein the make-up gas stream prepared in (i) is obtainable or obtained by a process comprising one or more of acetylene production, a gasification, steam reforming, and autothermal reforming of one or more of natural gas and biogas.

6. The process of claim 3 or 4, wherein the H2:CO2 molar ratio in the make-up gas stream prepared in (i) is in the range of from 1 :1 to 40:1.

7. The process of any one of claims 1 to 6, wherein the make-up gas stream prepared in (i) comprises from 50 to 80 volume-% of H2.

8. The process of any one of claims 1 to 7, wherein the make-up gas stream prepared in (i) comprises from 1 to 40 volume-%, of CO.

9. The process of any one of claims 1 to 8, wherein the H2:CO molar ratio in the make-up gas stream prepared in (i) is in the range of from 0.1 :1 to 100:1.

10. The process of any one of claims 1 to 9, wherein from 50 to 100 volume-%, of the CO2- containing gas stream prepared in (ii) consists of CO2.

11. The process of any one of claims 1 to 10, wherein from 50 to 100 volume-% of the (^-containing gas stream prepared in (iii) consists of H2.

12. The process of any one of claims 1 to 11 , wherein the H2:CO2 molar ratio in the reaction gas stream obtained from (iv) is in the range of from 3:1 to 20.0:1.

13. The process of any one of claims 1 to 12, wherein the H2:CO molar ratio in the reaction gas stream obtained from (iv) is in the range of from 1.0:1 to 5.0:1.

14. The process of any one of claims 1 to 13, wherein the CO:CC>2 molar ratio in the reaction gas stream obtained from (iv) is in the range of from 0.1:1 to 9.1 :1.

15. The process of any one of claims 1 to 14, wherein the reaction gas stream obtained from (iv) displays a S value of greater than 2.00, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2)) I (n(CO) + n(CO2)) (I).

16. The process of any one of claims 1 to 15, wherein the catalyst comprised in the reactor according to (v) comprises one or more of Cu, Zn, Al, Zr, Si, and O.

17. The process of any one of claims 1 to 16, wherein contacting according to (v) is performed at a temperature in the range of from 190 to 350 °C.

18. A process comprising a step of converting the methanol obtainable or obtained by the process according to any one of claims 1 to 17 to obtain a product Q.

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