Flexible syngas production by coupling reverse-water-gas-shift technology with a chemical process

Abstract

The present invention relates to a process for preparing and processing of synthesis gas, the process particularly comprising the steps of preparing a first gas stream comprises H2 and CO2; feeding said gas stream into a first reactor comprising a reverse water gas shift catalyst, wherein said gas stream is fed into the first reactor at a gas hourly space velocity (GHSV) in the range of from 1,000 to 100,000 h-1, wherein the reverse water gas shift reaction is conducted at a temperature in the range of from 650 to 1,000 °C, wherein in a time interval Δt, wherein Δt is in the range of from 1 to 60 minutes, the GHSV of said gas stream displays a gradient in the range of from 2,000 to 60,000 h-1, obtaining a second gas stream; feeding the second gas stream into a second reactor, wherein the second reactor comprises one or more of a methanol synthesis catalyst, a dimethyl ether synthesis catalyst, an oxo synthesis or hydroformylation catalyst, a Fischer-Tropsch synthesis catalyst, a formic acid synthesis catalyst, and a phosgene synthesis catalyst, obtaining a product stream.

Description

240940W001Flexible syngas production by coupling reverse-water-gas-shift technology with a chemical processTECHNICAL FIELDThe present invention relates to a flexible syngas production process participating in stabilizing an electric grid. The syngas is produced by a reverse water gas shift (rWGS) process and is fed, after dehydration, into a chemical process which is bigger, in particular in terms of a volume conversion, than the actual rWGS step. The rWGS process can be operated very flexibly with short adaption times at constant temperatures. Thus, in particular the rWGS process can participate in electric over- or under-capacities, which particularly allows for stabilizing the electric grid and preserving the coupled chemical processes from direct fluctuations.INTRODUCTIONThe reverse water gas shift (rWGS) reaction is an endothermic process (AHr(g) = +41.2 kJ / mol), which is formally described by equation (1). Since it is an equilibrium reaction, all reactants and CH4 as side-product are typically present. The rWGS reaction can generally be conducted under pressures of 1 to 20 bara and in the temperature range of 250 to 1000 °C. The syngas produced by the rWGS reaction could be used, e.g., for a methanol production.Industrially, methanol can be produced from a syngas mixture mainly comprising CO, CO2 and H2. The methanol production can be described by equations (1) to (3) and can be conducted at elevated pressures of 30 to 100 bar and temperatures between 190 and 300 °C. Such conditions generally relate a low-pressure methanol process, which is described in “Ullmann's Encyclopedia of Industrial Chemistry, Chapter-Methanol, 2012 Wiley-VCH”.CO2+ H2CO + H2O (1).CO + 2H2CH3OH (2).CO2+ 3H2CH3OH + H2O (3).For an optimized process, the syngas or make-up gas (MUG) of the methanol process should fulfill certain stoichiometric requirements that methanol is formed. Typically, a stoichiometric number S is used for defining the syngas or MUG in this respect, wherein S is calculated according to equation (4).240940W001- 2 -S = (n(H2) - n(CO2) / (n(CO) + n(CO2)) (4).Usually, the syngas or MUG is prepared having an S value of higher than 1 .95.The generation of renewable electricity is strongly dependent on the, e.g., solar and wind availability. This typically results in a fluctuating supply, which is not preferred for the electric grid, which needs stable operational conditions. Thus, the renewable energy supply has to be buffered and coupled to other applications for energy storage or conversions, like the electrolysis of water.WO 2023 / 41396 A1 relates to a method for producing syngas using a catalytic reverse water gas shift reaction. This application focuses on a rWGS process setup wherein two consecutive reactors are set for conducting the rWGS process at a temperature up to 600 °C.WO 2008 / 115933 A1 focuses on a rWGS process with a recycle process concept to produce mainly CO.WO 2021 / 062384 A1 focuses also on a rWGS process, wherein consecutive reactors are part of the process.C. Markowitsch et al. disclose a study on the impact of the operation conditions on the reverse- water-gas shift reaction in “Global Challenges for a Sustainable Society: EURECA-PRO the European University for Responsible Consumption and Production”. In particular, it would be disclosed therein that a reverse water gas shift reaction (rWGS) using a nickel-based catalyst can be applied in an end-to-end power-to-liquid chain.US 2024 / 002221 A1 relates to a method for producing syngas using a catalytic reverse water gas shift (rWGS) reaction, wherein the syngas would be suitable for a variety of subsequent conversion processes, such as methanol synthesis and Fischer-Tropsch synthesis.Thus, there was a need to provide a process allowing an integrating generation of renewable electricity into existing chemical processes, as for example production of methanol.DETAILED DESCRIPTION240940W001- 3 -As noted above, the electrolysis of water by regenerative power is a non-static process, where the hydrogen supply constantly fluctuates. This dynamic behavior influences downstream applications.It has surprisingly been found that integration of a hydrogen supply into a rWGS process can buffer the fluctuating character of the hydrogen supply, wherein the rWGS process can be operated by an electrified reactor-setup. Thus, it has been found that by coupling a specific rWGS process to a chemical process enables a process design, where the endothermic reaction can be ramped-up and ramped-down very fast, in particular reaching steady state conditions below 10 mins. As such, the rWGS reaction is able to actively moderate the electric grid as well.Thus, it has surprisingly been found that an rWGS process, which can be varied with respect to the volume flow rate, allows for actively moderating electric grid stability by balancing over- or under-capacities within cycles of for example 15 minutes. Coupling such a flexible rWGS application to a bigger chemical process like the MeOH production, surprisingly enables a comparatively normal methanol process, but fully coupled to the electric grid.Therefore, the present invention relates to a process for preparing and processing of synthesis gas, the process comprising(i) preparing a first gas stream S1 , wherein S1 comprises H2 and CO2, wherein S1 has a H2:CO2 molar ratio in the range of from 0.5:1 to 4:1 ;(ii) feeding S1 prepared in (i) into a first reactor comprising a reverse water gas shift catalyst, wherein S1 is fed into the first reactor at a gas hourly space velocity (GHSV) in the range of from 1 ,000 to 100,000 h’1, wherein the reverse water gas shift reaction is conducted at a temperature in the range of from 650 to 1 ,000 °C, wherein in a time interval At, wherein At is in the range of from 1 to 60 minutes, the GHSV of S1 displays a gradient in the range of from 2,000 to 60,000 h’1, obtaining a second gas stream S2, wherein S2 comprises CO, H2, CO2, and optionally H2O;(iii) optionally separating one or more of H2O, CO2, CH4 and H2 from S2;(iv) optionally combining S2 with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, obtaining a fifth gas stream S5;(v) feeding S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) into a second reactor, wherein the second reactor comprises one or more of a methanol synthesis catalyst, a dimethyl ether synthesis catalyst, an oxo synthesis or hydroformylation catalyst, a Fischer-Tropsch synthesis catalyst, a formic acid synthesis catalyst, and a phosgene synthesis catalyst,240940W001- 4 - obtaining a product stream.Depending on which catalyst(s) are used, the product may be one or more methanol, dimethyl ether, an aldehyde, an alkane, formic acid, and phosgene.In the context of the present invention, the time interval At designates a period during the process from any point in time t1 to any later point in time t2, wherein At = t2 - 11.It is preferred that preparing S1 according to (i) comprises combining a ^-containing stream and a CCh-containing stream.In the case wherein preparing S1 according to (i) comprises combining a ^-containing stream and a CCh-containing stream, it is preferred that the ^-containing stream is obtainable or obtained by a process comprising one or more of water electrolysis, NHs-reforming, more preferably green NHs-reforming, propane dehydrogenation, iso-butane dehydrogenation, steam reforming, more preferably steam reforming of natural gas or bio-gas or bio-methane, and autothermal reforming of natural gas or biogas or bio-methane.Further in the case wherein preparing S1 according to (i) comprises combining a ^-containing stream and a CCh-containing stream, it is preferred that from 99 to 100 volume-%, more preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the ^-containing stream consist of H2.Further in the case wherein preparing S1 according to (i) comprises combining a ^-containing stream and a CCh-containing stream, it is preferred that the CCh-containing stream is obtainable or obtained by a chemical production plant, more preferably by one or more of a power plant, a steam cracker, an ethylene oxide production plant, an acetylene production plant, an ammonia plant, an incineration process, a bio-process, and air, or wherein the CCh-containing stream is obtainable or obtained by a process comprising one or more of CO2 capture, NH3 production, hydrogen production, refining, cement production, lime production, glass production, aluminum smelting, iron smelting, and ferro-alloy production.Further in the case wherein preparing S1 according to (i) comprises combining a H2-containing stream and a CCh-containing stream, it is preferred that the CCh-containing stream comprises an inert gas, wherein the inert gas more preferably comprises one or more of N2, and Ar, more preferably N2.240940W001- 5 -In the case wherein the CCh-containing stream comprises an inert gas, it is preferred that the CC>2-containing stream comprises from 0 to 2 volume-%, more preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of the inert gas.Further in the case wherein preparing S1 according to (i) comprises combining a (^-containing stream and a CCh-containing stream, it is preferred that the CCh-containing stream comprises CH4, wherein the CCh-containing stream preferably comprises from 0 to 5 volume-%, more preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of CH4.Further in the case wherein preparing S1 according to (i) comprises combining a (^-containing stream and a CCh-containing stream, it is preferred that from 98 to 100 volume-%, more preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the CCh-con- taining stream consist of CO2 and optionally an inert gas.It is preferred that S1 prepared in (i) has a F^CCh molar ratio in the range of from 1.0:1 to 3.0:1 , preferably in the range of from 1.5:1 to 2.5:1 , more preferably in the range of from 1.9:1 to 2.1 :1.It is preferred that the first reactor according to (ii) has an inlet and an outlet and wherein S1 prepared in (i) is fed into the first reactor at the inlet.It is preferred that the first reactor according to (ii) is electrically heated, wherein electricity for electrically heating the first reactor according to (ii) is more preferably obtained or obtainable by one or more of geothermal sources, solar power, wind energy, hydro-power, combustion of waste, and off-peak power grid supplies.It is preferred that the reverse water gas shift catalyst comprised in the first reactor according to (ii) comprises Ni.In the case wherein the reverse water gas shift catalyst comprised in the first reactor according to (ii) comprises Ni, it is preferred that the reverse water gas shift catalyst contained in the first reactor further comprises a metal M selected from the group consisting of alkali metals, alkaline earth metals, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of Li, K, Na, Cs, Mg, Ca, Sr, Ba, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of K, Na, Cs, Ba, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of K, Ba, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of Fe, Ru, or Fe and Ru, wherein more preferably M comprises Ru, wherein more preferably M is Ru.240940W001- 6 -Further in the case wherein the reverse water gas shift catalyst comprised in the first reactor according to (ii) comprises Ni, it is preferred that the reverse water gas shift catalyst contained in the first reactor according to (ii) further comprises one or more support materials onto which the Ni or the metal M are supported, wherein the one or more support materials are preferably selected from the group consisting of AI2O3, SiC>2, ZrC>2, CeC>2, MgO, CaO, and mixtures of two or more thereof, more preferably from the group consisting of AI2O3, SiC>2, ZrC>2, CeC>2, and mixtures of two or more thereof, more preferably from the group consisting of AI2O3, SiC>2, and mixtures thereof, wherein more preferably the support material comprises AI2O3.In the case wherein the reverse water gas shift catalyst contained in the first reactor further comprises a metal M selected from the group consisting of alkali metals, alkaline earth metals, Mo, Fe, and Ru, including mixtures of two or more thereof, it is preferred that the reverse water gas shift catalyst contained in the first reactor according to (ii) displays an M : Ni atomic ratio in the range of from 0.1 :99.9 to 80:20, more preferably of from 0.5:99.5 to 75:25, more preferably of from 1 :99 to 70:30, more preferably of from 5:95 to 65:35, more preferably of from 15:85 to 60:40, more preferably of from 30:70 to 55:45, and more preferably of from 40:60 to 50:50.In the case wherein the reverse water gas shift catalyst contained in the first reactor according to (ii) displays an M : Ni atomic ratio in the range of from 0.1 :99.9 to 80:20, it is preferred according to a first alternative that M comprises, preferably is, Fe, and that the reverse water gas shift catalyst displays an M : Ni atomic ratio in the range of from 1 :99 to 80:20, more preferably of from 5:95 to 75:25, more preferably of from 10:90 to 70:30, more preferably of from 20:80 to 65:35, more preferably of from 30:70 to 60:40, more preferably of from 35:65 to 55:45, and more preferably of from 40:60 to 50:50.Further in the case wherein the reverse water gas shift catalyst contained in the first reactor according to (ii) displays an M : Ni atomic ratio in the range of from 0.1 :99.9 to 80:20, it is preferred according to a second alternative that M comprises, preferably is, Ru, and that the reverse water gas shift catalyst displays an M : Ni atomic ratio in the range of from 0.1 :99.9 to 30:70, more preferably of from 0.5:99.5 to 30:70, more preferably of from 1 :99 to 20:80, more preferably of from 3:97 to 10:90, and more preferably of from 5:95 to 6:94.Further in the case wherein the reverse water gas shift catalyst comprised in the first reactor according to (ii) comprises Ni, it is preferred that the reverse water gas shift catalyst contained in the first reactor according to (ii) further comprises Al and O.240940W001- 7 -In the case wherein the reverse water gas shift catalyst contained in the first reactor according to (ii) further comprises Al and O, it is preferred that the reverse water gas shift catalyst further comprises Mg, wherein the Ni : Mg : Al molar ratio is more preferably in the range of from 1 : (0.1 - 12) : (0.5 - 20), more preferably of from 1 : (0.5 - 8) : (1 - 12), more preferably of from 1 : (1 - 5) : (3 - 8), more preferably of from 1 : (1 .5 - 3) : (3.5 - 5), and more preferably of from 1 : (2.0 - 2.4) : (4.0 - 4.4).In the case wherein the reverse water gas shift catalyst further comprises Mg, wherein the Ni : Mg : Al molar ratio is more preferably in the range of from 1 : (0.1 - 12) : (0.5 - 20), it is preferred according to a first alternative that from 95 to 100 weight-% of the reverse water gas shift catalyst consists of Ni, Mg, Al, 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-%, and more preferably from 99.9 to 100 weight-%.Further in the case wherein the reverse water gas shift catalyst further comprises Mg, wherein the Ni : Mg : Al molar ratio is more preferably in the range of from 1 : (0.1 - 12) : (0.5 - 20), it is preferred according to a second alternative that from 95 to 100 weight-% of the reverse water gas shift catalyst consists of M, Ni, Mg, Al, and O, more preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.It is preferred that S1 is fed into the first reactor according to (ii) at a gas hourly space velocity (GHSV) in the range of from 5,000 to 75,000 h’1, more preferably of from 10,000 to 50,000 h’1, more preferably of from 15,000 to 25,000 h’1.It is preferred that the reverse water gas shift reaction is conducted according to (ii) at a temperature in the range of from 750 to 975 °C, more preferably in the range of from 775 to 960 °C, more preferably in the range of from 800 to 940 °C, more preferably in the range of from 825 to 920 °C, more preferably in the range of from 850 to 890 °C.It is preferred that the reverse water gas shift reaction is conducted according to (ii) at a pressure in the range of from 2 to 25 bara, more preferably in the range of from 3 to 23 bara, more preferably in the range of from 5 to 18 bara, more preferably in the range of from 6 to 16 bara, more preferably in the range of from 8 to 14 bara, more preferably in the range of from 9 to 13 bara.It is preferred that At according to (ii) is in the range of from 5 to 45 minutes, more preferably of from 5 to 30 minutes, more preferably of from 10 to 15 minutes.240940W001- 8 -It is preferred that the GHSV of S1 displays a gradient in the time interval At according to (ii) in the range of from 3,000 to 40,000 h’1, more preferably of from 4,000 to 30,000 h’1, more preferably of from 5,000 to 20,0000 h’1.It is preferred that during the time interval At in (ii), the reaction temperature is maintained between a maximum temperature Tmax and a minimum temperature Tmin, wherein AT = Tmax - Tmin is in the range of from 0 to 25 K, more preferably of from 0 to 20 K, more preferably of from 0 to 15 K, more preferably of from 0 to 10 K, more preferably from 0 to 5 K.It is preferred that no recycle stream obtainable or obtained from the product stream is fed into S1 , wherein more preferably no recycle stream is fed into the first reactor according to (ii).It is preferred that S2 obtained from (ii) comprises from 15.0 to 50.0 volume-%, more preferably from 26.0 to 33.0 volume-%, more preferably from 28.0 to 31 .0 volume-%, of CO.It is preferred that S2 obtained from (ii) comprises from 20.0 to 75.0 volume-%, more preferably from 49.0 to 60.0 volume-%, more preferably from 52.0 to 56.5 volume-%, of H2.It is preferred that S2 obtained from (ii) comprises from 5.0 to 35.0 volume-%, more preferably from 12.0 to 18.0 volume-%, more preferably from 14.0 to 16.0 volume-%, of CO2.It is preferred that S2 obtained from (ii) further comprises CH4, wherein S2 obtained from (ii) more preferably comprises from 0.5 to 15 volume-%, more preferably from 0.8 to 1.6 volume-%, more preferably from 1 .0 to 5 volume-%, of CH4.It is preferred that S2 obtained from (ii) further comprises H2O, wherein S2 obtained from (ii) more preferably comprises from 5 to 35 volume-%, more preferably from 0 to 0.01 volume-%, more preferably from 0 to 0.001 volume-%, of H2O.It is preferred that S2 obtained from (ii) has a volume flow rate in the range of from 100 to 200,000 Nm3 / h, more preferably in the range of from 150 to 100,000 Nm3 / h, more preferably in the range of from 200 to 50,000 Nm3 / h, more preferably in the range of from 250 to 17,500 Nm3 / h, more preferably in the range of from 400 to 15,100 Nm3 / h.It is preferred that S2 obtained from (ii) further comprises H2O, and wherein the process further comprises after (ii) and prior to (iii), (iv) or (v)(ii’) Separating at least a portion of H2O from S2 obtained from (ii).240940W001- 9 -It is preferred that S2 obtained from (ii) or (ii’), more preferably obtained from (ii’), comprises from 23.0 to 36.0 volume-%, more preferably from 26.0 to 33.0 volume-%, more preferably from 28.0 to 31.0 volume-%, of CO.It is preferred that S2 obtained from (ii) or (ii’), more preferably obtained from (ii’), comprises from 44.0 to 65.0 volume-%, more preferably from 49.0 to 60.0 volume-%, more preferably from 52.0 to 56.5 volume-%, of H2.It is preferred that S2 obtained from (ii) or (ii’), more preferably obtained from (ii’), comprises from 10.0 to 20.0 volume-%, more preferably from 12.0 to 18.0 volume-%, more preferably from 14.0 to 16.0 volume-%, of CO2.It is preferred that S2 obtained from (ii) or (ii’), more preferably obtained from (ii’), further comprises CH4, wherein S2 obtained from (ii) or (ii’) more preferably comprises from 0.5 to 1.9 vol- ume-%, more preferably from 0.8 to 1.6 volume-%, more preferably from 1.0 to 1.4 volume-%, of CH4.It is preferred that S2 obtained from (ii) or (ii’), more preferably obtained from (ii’), further comprises H2O, wherein S2 obtained from (ii) or (ii’) more preferably comprises from 0 to 0.1 vol- ume-%, more preferably from 0 to 0.01 volume-%, more preferably from 0 to 0.001 volume-%, of H2O.It is preferred that S2 obtained from (ii) or (ii’), more preferably obtained from (ii’), has a volume flow rate in the range of from 100 to 200,000 Nm3 / h, more preferably in the range of from 150 to 100,000 Nm3 / h, more preferably in the range of from 200 to 50,000 Nm3 / h, more preferably in the range of from 250 to 17,500 Nm3 / h, more preferably in the range of from 400 to 15,100 Nm3 / h.It is preferred that one or more of CO2, CH4, and H2 are separated from S2 according to (iii), wherein more preferably H2 is separated from S2 according to (iii), wherein more preferably CO2 and H2 are separated from S2 according to (iii), wherein more preferably CO2, CH4, and H2 are separated from S2 according to (iii), wherein the process more preferably comprises (ii’) as defined in embodiment 36.It is preferred that one or more of H2O, CO2, CH4, and H2 are separated from S2 according to (iii), wherein more preferably H2O is separated from S2 according to (iii), wherein more preferably H2O and H2 are separated from S2 according to (iii), wherein more preferably H2O, CO2, and240940W001- 10 -H2 are separated from S2 according to (iii), wherein more preferably H2O, CO2, CH4, and H2 are separated from S2 according to (iii).It is preferred that the second reactor according to (v) has an inlet and an outlet and wherein S2 obtained from (ii), S2 obtained from (ii’), or S6 obtained from (iv) is fed into the second reactor at the inlet.It is preferred that the process comprising combining S2 with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, obtaining a fifth gas stream S5, according to (iv), wherein (iv) more preferably comprisesCombining S2 obtained from (ii) or (ii’) with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, preferably the recycle stream obtained from the second reactor as defined herein.It is preferred that the process further comprises after (ii), preferably after (ii’), and prior to (iv) (iii’) preparing a third gas stream S3, wherein S3 comprises H2, wherein S3 is more preferably obtainable or obtained by a process comprising one or more of water electrolysis, NHs-reforming, preferably green NHs-reforming, steam reforming, preferably steam reforming of natural gas or bio-gas or bio-methane, and autothermal reforming of natural gas or bio-gas or bio-methane.In the case wherein the process further comprises after (ii), preferably after (ii’), and prior to (iv) preparing a third gas stream S3, wherein S3 comprises H2, according to (iii’), it is preferred that from 99 to 100 volume-%, more preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of S3 prepared in (iii’) consist of H2.Further in the case wherein the process further comprises after (ii), preferably after (ii’), and prior to (iv) preparing a third gas stream S3, wherein S3 comprises H2, according to (iii’), it is preferred that S3 prepared in (iii’) has a volume flow rate in the range of from 10,000 to 150,000 Nm3 / h, more preferably in the range of from 20,000 to 100,000 Nm3 / h, more preferably in the range of from 25,000 to 43,500 Nm3 / h, more preferably in the range of from 26,500 to 34,200 Nm3 / h.It is preferred that the process further comprises after (ii), preferably after (ii’), and prior to (iv) (iii”) preparing a fourth gas stream S4, wherein S4 comprises CO2, wherein S4 is more preferably obtainable or obtained by one or more of a power plant, a steam cracker, an ammonia plant, an incineration process, a bio-process, and air, or wherein S4 is obtainable or240940W001- 11 - obtained by a process comprising one or more of CO2 capture, NH3 production, hydrogen production, refining, cement production, lime production, glass production, aluminum smelting, iron smelting, and ferro-alloy production.In the case wherein the process further comprises after (ii), preferably after (ii’), and prior to (iv) preparing a fourth gas stream S4, wherein S4 comprises CO2, according to (iii”), it is preferred that S4 prepared in (iii”) comprises an inert gas, wherein the inert gas more preferably comprises one or more of N2 and Ar, more preferably N2.In the case wherein S4 prepared in (iii”) comprises an inert gas, it is preferred that S4 prepared in (iii”) comprises from 0 to 2 volume-%, more preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of the inert gas.Further in the case wherein S4 prepared in (iii”) comprises an inert gas, it is preferred that S4 prepared in (iii”) comprises CH4, wherein S4 prepared in (iii”) comprises from 0 to 5 volume-%, more preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of CH4.Further in the case wherein S4 prepared in (iii”) comprises an inert gas, it is preferred that from 98 to 100 volume-%, more preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of S4 prepared in (iii”) consist of CO2 and optionally an inert gas.Further in the case wherein S4 prepared in (iii”) comprises an inert gas, it is preferred that S4 prepared in (iii”) has a volume flow rate in the range of from 1 ,000 to 50,000 Nm3 / h, more preferably in the range of from 2,000 to 20,000 Nm3 / h, more preferably in the range of from 5,000 to 14,000 Nm3 / h, more preferably in the range of from 8,000 to 10,000 Nm3 / h.It is preferred that the recycle stream is obtained from the second reactor, and wherein the recycle stream comprises one or more of H2, CO, H2O, CH3OH, N2, CH4, and CO2, more preferably one or more of H2, CO, and CO2.It is preferred that the recycle stream has an S value of greater than 2.30, more preferably in the range of from 2.30 to 7.00, 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 recycle stream, preferably the recycle stream obtained from the second reactor, more preferably the recycle stream obtained from the second reactor as defined in em-240940W001- 12 - bodiment 56, has a volume flow rate in the range of from 10,000 to 500,000 Nm3 / h, more preferably in the range of from 50,000 to 200,000 Nm3 / h, more preferably in the range of from 100,000 to 150,000 Nm3 / h, more preferably in the range of from 122,000 to 201 ,500 Nm3 / h.It is preferred that S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) is fed according to (v) into the second reactor having a volume flow rate in the range of from 5,000 to 1 ,000,000 Nm3 / h, more preferably in the range of from 50,000 to 500,000 Nm3 / h, more preferably in the range of from 100,000 to 300,000 Nm3 / h, more preferably in the range of from 158,000 to 260,900 Nm3 / h.It is preferred that S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) has an S value of greater than 2.50, more preferably of greater than 3.50, more preferably in the range of from 3.50 to 4.40, more preferably in the range of from 3.70 to 4.20, more preferably in the range of from 3.75 to 4.15, in the second reactor, more preferably at the inlet of the second reactor, wherein the S value is calculated according to formula (II)S = (n(H2) - n(CO2) I (n(CO) + n(CO2)) (II).It is preferred that the product stream comprises one or more of H2, CO2, and CO, more preferably one or more of H2, CO2, CO, H2O, CH3OH, and one or more alkanes, more preferably one or more of H2, CO2, CO, H2O, CH3OH, dimethyl ether, formic acid, phosgene, one or more aldehydes, and one or more alkanes.In the case wherein the product stream comprises one or more of H2, CO2, and CO, it is preferred that the process further comprises(vi) separating one or more of H2, CO2, and CO from the product stream obtained from (v), obtaining a sixth gas stream S6, wherein S6 comprises one or more of H2, CO2, and CO.In the case wherein the process further comprises separating one or more of H2, CO2, and CO from the product stream obtained from (v), obtaining a sixth gas stream S6, wherein S6 comprises one or more of H2, CO2, and CO according to (vi), it is preferred that the process further comprises after (vi)(vii) recycling at least a portion of S6 obtained from (vi) into the recycle stream according to (iv).It is preferred that the second reactor according to (v) comprises a methanol synthesis catalyst.240940W001- 13 -In the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises one or more of Cu, Zn, Al, Zr, Si, and O, more preferably Cu, Zn, Al, Zr, Si, and O.Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises elemental copper.Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises Zn and Si, wherein the methanol synthesis catalyst comprised in the second reactor 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.Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises one or more oxides of Zn, Al, Zr, and Si, wherein the methanol synthesis catalyst more preferably comprises one or more oxides selected from the group consisting of ZnO, ZnAhOt, and CUAI2O4, wherein more preferably the methanol synthesis catalyst comprises ZnO and ZnAhO4, or ZnO and CUAI2O4, or ZnO, ZnAhO4, and CUAI2O4.Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor 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 preferably determined according to Reference Example 1.Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises Cu, wherein the methanol synthesis catalyst comprised in the second reactor according to (vii) 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 determined according to Reference Example 2.Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises SiC>2.240940W001- 14 -Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that the methanol synthesis catalyst comprised in the second reactor comprises Cu, Zn, Al, Zr, and Si, wherein the methanol synthesis catalyst comprised in the second reactor 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).Further in the case wherein the second reactor according to (v) comprises a methanol synthesis catalyst, it is preferred that from 95 to 100 weight-% of the methanol synthesis catalyst comprised in the second reactor 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 S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) fed into a second reactor are subjected in the second reactor to reaction conditions, wherein the reaction comprises one or more of a methanol synthesis, a dimethyl ether synthesis, an oxo synthesis, a Fischer-Tropsch synthesis, a formic acid synthesis, and a phosgene synthesis.It is preferred that a methanol synthesis is conducted in the second reactor according to (v), wherein the product stream comprises methanol.In the case wherein a methanol synthesis is conducted in the second reactor according to (v), wherein the product stream comprises methanol, it is preferred that the methanol synthesis is conducted in the second reactor according to (v) at a temperature in the range of from 190 to 280 °C, more preferably in the range of from 210 to 260 °C, more preferably in the range of from 225 to 245 °C.Further in the case wherein a methanol synthesis is conducted in the second reactor according to (v), wherein the product stream comprises methanol, it is preferred that the methanol synthesis is conducted in the second reactor according to (v) at a pressure in the range of from 65 to 85 bara, more preferably in the range of from 70 to 80 bara, more preferably in the range of from 73 to 77 bara.240940W001- 15 -Further, the present invention relates to a process, preferably the process according to any one of the embodiments disclosed herein, comprising a step of converting the product comprised in the product stream, preferably methanol, obtainable or obtained by the process according to any one of the embodiments disclosed herein to obtain a product Q. Yet further, the present invention relates to a process comprising the step of using the product, preferably 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 C-containing product comprised in the product stream 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-%240940W001- 16 - 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 C-containing product comprised in the product stream 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 group240940W001- 17 - 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; in particular 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 RF1.240940W001- 18 -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 surfactants 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 conducted240940W001- 19 - 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 be performed 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 RF1.240940W001- 20 -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 RF1.240940W001- 21 -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) coated240940W001- 22 - 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 Die-240940W001- 23 - tionary 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 ingredient refers 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 (also abbreviated as bar(abs)) refers to an absolute pressure and the unit barg (also abbreviated as bar(gauge)) to a relative 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 and processing of synthesis gas, the process comprising(i) preparing a first gas stream S1 , wherein S1 comprises H2 and CO2, wherein S1 has a H2:CC>2 molar ratio in the range of from 0.5:1 to 4:1 ;(ii) feeding S1 prepared in (i) into a first reactor comprising a reverse water gas shift catalyst, wherein S1 is fed into the first reactor at a gas hourly space velocity (GHSV) in the range of from 1 ,000 to 100,000 h’1, wherein the reverse water gas shift reaction is conducted at a temperature in the range of from 650 to 1 ,000 °C,240940W001- 24 - wherein in a time interval At, wherein At is in the range of from 1 to 60 minutes, the GHSV of S1 displays a gradient in the range of from 2,000 to 60,000 h’1, obtaining a second gas stream S2, wherein S2 comprises CO, H2, CO2, and optionally H2O;(iii) optionally separating one or more of H2O, CO2, CH4 and H2 from S2;(iv) optionally combining S2 with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, obtaining a fifth gas stream S5;(v) feeding S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) into a second reactor, wherein the second reactor comprises one or more of a methanol synthesis catalyst, a dimethyl ether synthesis catalyst, an oxo synthesis or hydroformylation catalyst, a Fischer-Tropsch synthesis catalyst, a formic acid synthesis catalyst, and a phosgene synthesis catalyst, obtaining a product stream.2. The process of embodiment 1 , wherein preparing S1 according to (i) comprises combining a H2-containing stream and a CCh-containing stream.3. The process of embodiment 2, wherein the ^-containing stream is obtainable or obtained by a process comprising one or more of water electrolysis, NHs-reforming, preferably green NHs-reforming, propane dehydrogenation, iso-butane dehydrogenation, steam reforming, preferably steam reforming of natural gas or bio-gas or bio-methane, and autothermal reforming of natural gas or biogas or bio-methane.4. The process of embodiment 2 or 3, wherein from 99 to 100 volume-%, preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the ^-containing stream consist of H2.5. The process of any one of embodiments 2 to 4, wherein the CCh-containing stream is obtainable or obtained by a chemical production plant, preferably by one or more of a power plant, a steam cracker, an ethylene oxide production plant, an acetylene production plant, an ammonia plant, an incineration process, a bio-process, and air, or wherein the CO2- containing stream is obtainable or obtained by a process comprising one or more of CO2 capture, NH3 production, hydrogen production, refining, cement production, lime production, glass production, aluminum smelting, iron smelting, and ferro-alloy production.240940W001- 25 -6. The process of any one of embodiments 2 to 5, wherein the CCh-containing stream comprises an inert gas, wherein the inert gas preferably comprises one or more of N2, and Ar, more preferably N2.7. The process of embodiment 6, wherein the CCh-containing stream comprises from 0 to 2 volume-%, preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of the inert gas.8. The process of any one of embodiments 2 to 7, wherein the CCh-containing stream comprises CH4, wherein the CCh-containing stream preferably comprises from 0 to 5 volume- %, more preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of CH4.9. The process of any one of embodiments 2 to 8, wherein from 98 to 100 volume-%, preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of the CO2- containing stream consist of CO2 and optionally an inert gas.10. The process of any one of embodiments 1 to 9, wherein S1 prepared in (i) has a H2:CO2 molar ratio in the range of from 1.0:1 to 3.0:1, preferably in the range of from 1.5:1 to 2.5:1, more preferably in the range of from 1.9:1 to 2.1:1.11. The process of any one of embodiments 1 to 10, wherein the first reactor according to (ii) has an inlet and an outlet and wherein S1 prepared in (i) is fed into the first reactor at the inlet.12. The process of any one of embodiments 1 to 11, wherein the first reactor according to (ii) is electrically heated, wherein electricity for electrically heating the first reactor according to (ii) is preferably obtained or obtainable by one or more of geothermal sources, solar power, wind energy, hydro-power, combustion of waste, and off-peak power grid supplies.13. The process of any one of embodiments 1 to 12, wherein the reverse water gas shift catalyst comprised in the first reactor according to (ii) comprises Ni.14. The process of embodiment 13, wherein the reverse water gas shift catalyst contained in the first reactor further comprises a metal M selected from the group consisting of alkali metals, alkaline earth metals, Mo, Fe, and Ru, including mixtures of two or more thereof, preferably from the group consisting of Li, K, Na, Cs, Mg, Ca, Sr, Ba, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of K,240940W001- 26 -Na, Cs, Ba, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of K, Ba, Mo, Fe, and Ru, including mixtures of two or more thereof, more preferably from the group consisting of Fe, Ru, or Fe and Ru, wherein more preferably M comprises Ru, wherein more preferably M is Ru.15. The process of embodiment 13 or 14, wherein the reverse water gas shift catalyst contained in the first reactor according to (ii) further comprises one or more support materials onto which the Ni or the metal M are supported, wherein the one or more support materials are preferably selected from the group consisting of AI2O3, SiC>2, ZrC>2, CeC>2, MgO, CaO, and mixtures of two or more thereof, more preferably from the group consisting of AI2O3, SiC>2, ZrC>2, CeC>2, and mixtures of two or more thereof, more preferably from the group consisting of AI2O3, SiC>2, and mixtures thereof, wherein more preferably the support material comprises AI2O3.16. The process of embodiment 14 or 15, wherein the reverse water gas shift catalyst contained in the first reactor according to (ii) displays an M : Ni atomic ratio in the range of from 0.1 :99.9 to 80:20, preferably of from 0.5:99.5 to 75:25, more preferably of from 1 :99 to 70:30, more preferably of from 5:95 to 65:35, more preferably of from 15:85 to 60:40, more preferably of from 30:70 to 55:45, and more preferably of from 40:60 to 50:50.17. The process of embodiment 16, wherein M comprises, preferably is, Fe, and wherein the reverse water gas shift catalyst displays an M : Ni atomic ratio in the range of from 1 :99 to 80:20, preferably of from 5:95 to 75:25, more preferably of from 10:90 to 70:30, more preferably of from 20:80 to 65:35, more preferably of from 30:70 to 60:40, more preferably of from 35:65 to 55:45, and more preferably of from 40:60 to 50:50.18. The process of embodiment 16 or 17, wherein M comprises, preferably is, Ru, and wherein the reverse water gas shift catalyst displays an M : Ni atomic ratio in the range of from 0.1 :99.9 to 30:70, preferably of from 0.5:99.5 to 30:70, more preferably of from 1 :99 to 20:80, more preferably of from 3:97 to 10:90, and more preferably of from 5:95 to 6:94.19. The process of any one of embodiments 13 to 18, wherein the reverse water gas shift catalyst contained in the first reactor according to (ii) further comprises Al and O.20. The process of embodiment 19, wherein the reverse water gas shift catalyst further comprises Mg, wherein the Ni : Mg : Al molar ratio is preferably in the range of from 1 : (0.1 - 12) : (0.5 - 20), more preferably of from 1 : (0.5 - 8) : (1 - 12), more preferably of from 1 :240940W001- 27 -(1 - 5) : (3 - 8), more preferably of from 1 : (1.5 - 3) : (3.5 - 5), and more preferably of from 1 : (2.0 - 2.4) : (4.0 - 4.4).21. The process of embodiment 20, wherein from 95 to 100 weight-% of the reverse water gas shift catalyst consists of Ni, Mg, Al, 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-%, and more preferably from 99.9 to 100 weight-%.22. The process of embodiment 20, wherein from 95 to 100 weight-% of the reverse water gas shift catalyst consists of M, Ni, Mg, Al, and O, preferably from 97 to 100 wt.-%, more preferably from 98 to 100 wt.-%, more preferably from 99 to 100 wt.-%, more preferably from 99.5 to 100 wt.-%, and more preferably from 99.9 to 100 wt.-%.23. The process of any one of embodiments 1 to 22, wherein S1 is fed into the first reactor according to (ii) at a gas hourly space velocity (GHSV) in the range of from 5,000 to 75,000 h’1, preferably of from 10,000 to 50,000 h’1, more preferably of from 15,000 to 25,000 h’1.24. The process of any one of embodiments 1 to 23, wherein the reverse water gas shift reaction is conducted according to (ii) at a temperature in the range of from 750 to 975 °C, more preferably in the range of from 775 to 960 °C, more preferably in the range of from 800 to 940 °C, more preferably in the range of from 825 to 920 °C, more preferably in the range of from 850 to 890 °C.25. The process of any one of embodiments 1 to 24, wherein the reverse water gas shift reaction is conducted according to (ii) at a pressure in the range of from 2 to 25 bara, preferably in the range of from 3 to 23 bara, more preferably in the range of from 5 to 18 bara, more preferably in the range of from 6 to 16 bara, more preferably in the range of from 8 to 14 bara, more preferably in the range of from 9 to 13 bara.26. The process of any one of embodiments 1 to 25, wherein At according to (ii) is in the range of from 5 to 45 minutes, preferably of from 5 to 30 minutes, more preferably of from 10 to 15 minutes.27. The process of any one of embodiments 1 to 26, wherein the GHSV of S1 displays a gradient in the time interval At according to (ii) in the range of from 3,000 to 40,000 h’1, preferably of from 4,000 to 30,000 h’1, more preferably of from 5,000 to 20,0000 h’1.240940W001- 28 -28. The process of any one of embodiments 1 to 27, wherein during the time interval At in (ii), the reaction temperature is maintained between a maximum temperature Tmax and a minimum temperature Tmin, wherein AT = Tmax - Tmin is in the range of from 0 to 25 K, preferably of from 0 to 20 K, more preferably of from 0 to 15 K, more preferably of from 0 to 10 K, more preferably from 0 to 5 K.29. The process of any one of embodiments 1 to 28, wherein no recycle stream obtainable or obtained from the product stream is fed into S1 , wherein preferably no recycle stream is fed into the first reactor according to (ii).30. The process of any one of embodiments 1 to 29, wherein S2 obtained from (ii) comprises from 15.0 to 50.0 volume-%, preferably from 26.0 to 33.0 volume-%, more preferably from 28.0 to 31.0 volume-%, of CO.31 . The process of any one of embodiments 1 to 30, wherein S2 obtained from (ii) comprises from 20.0 to 75.0 volume-%, preferably from 49.0 to 60.0 volume-%, more preferably from 52.0 to 56.5 volume-%, of H2.32. The process of any one of embodiments 1 to 31 , wherein S2 obtained from (ii) comprises from 5.0 to 35.0 volume-%, preferably from 12.0 to 18.0 volume-%, more preferably from 14.0 to 16.0 volume-%, of CO2.33. The process of any one of embodiments 1 to 32, wherein S2 obtained from (ii) further comprises CH4, wherein S2 obtained from (ii) preferably comprises from 0.5 to 15 volume- %, more preferably from 0.8 to 1.6 volume-%, more preferably from 1.0 to 5 volume-%, of CH4.34. The process of any one of embodiments 1 to 33, wherein S2 obtained from (ii) further comprises H2O, wherein S2 obtained from (ii) preferably comprises from 5 to 35 volume- %, more preferably from 0 to 0.01 volume-%, more preferably from 0 to 0.001 volume-%, of H2O.35. The process of any one of embodiments 1 to 34, wherein S2 obtained from (ii) has a volume flow rate in the range of from 100 to 200,000 Nm3 / h, preferably in the range of from 150 to 100,000 Nm3 / h, more preferably in the range of from 200 to 50,000 Nm3 / h, more preferably in the range of from 250 to 17,500 Nm3 / h, more preferably in the range of from 400 to 15,100 Nm3 / h.240940W001- 29 -36. The process of any one of embodiments 1 to 35, wherein S2 obtained from (ii) further comprises H2O, and wherein the process further comprises after (ii) and prior to (iii), (iv) or (v)(ii’) Separating at least a portion of H2O from S2 obtained from (ii).37. The process of any one of embodiments 1 to 36, wherein S2 obtained from (ii) or (ii’), preferably obtained from (ii’), comprises from 23.0 to 36.0 volume-%, preferably from 26.0 to 33.0 volume-%, more preferably from 28.0 to 31.0 volume-%, of CO.38. The process of any one of embodiments 1 to 37, wherein S2 obtained from (ii) or (ii’), preferably obtained from (ii’), comprises from 44.0 to 65.0 volume-%, preferably from 49.0 to 60.0 volume-%, more preferably from 52.0 to 56.5 volume-%, of H2.39. The process of any one of embodiments 1 to 38, wherein S2 obtained from (ii) or (ii’), preferably obtained from (ii’), comprises from 10.0 to 20.0 volume-%, preferably from 12.0 to 18.0 volume-%, more preferably from 14.0 to 16.0 volume-%, of CO2.40. The process of any one of embodiments 1 to 39, wherein S2 obtained from (ii) or (ii’), preferably obtained from (ii’), further comprises CH4, wherein S2 obtained from (ii) or (ii’) preferably comprises from 0.5 to 1.9 volume-%, more preferably from 0.8 to 1.6 volume-%, more preferably from 1.0 to 1 .4 volume-%, of CH4.41 . The process of any one of embodiments 1 to 40, wherein S2 obtained from (ii) or (ii’), preferably obtained from (ii’), further comprises H2O, wherein S2 obtained from (ii) or (ii’) preferably comprises from 0 to 0.1 volume-%, more preferably from 0 to 0.01 volume-%, more preferably from 0 to 0.001 volume-%, of H2O.42. The process of any one of embodiments 1 to 41 , wherein S2 obtained from (ii) or (ii’), preferably obtained from (ii’), has a volume flow rate in the range of from 100 to 200,000 Nm3 / h, preferably in the range of from 150 to 100,000 Nm3 / h, more preferably in the range of from 200 to 50,000 Nm3 / h, more preferably in the range of from 250 to 17,500 Nm3 / h, more preferably in the range of from 400 to 15,100 Nm3 / h.43. The process of any one of embodiments 1 to 42, wherein one or more of CO2, CH4, and H2 are separated from S2 according to (iii), wherein preferably H2 is separated from S2 according to (iii), wherein more preferably CO2 and H2 are separated from S2 according to (iii), wherein more preferably CO2, CH4, and H2 are separated from S2 according to (iii), wherein the process more preferably comprises (ii’) as defined in embodiment 36.240940W001- 30 -44. The process of any one of embodiments 1 to 43, wherein one or more of H2O, CO2, CH4, and H2 are separated from S2 according to (iii), wherein preferably H2O is separated from S2 according to (iii), wherein more preferably H2O and H2 are separated from S2 according to (iii), wherein more preferably H2O, CO2, and H2 are separated from S2 according to (iii), wherein more preferably H2O, CO2, CH4, and H2 are separated from S2 according to (iii).45. The process of any one of embodiments 1 to 44, wherein the second reactor according to (v) has an inlet and an outlet and wherein S2 obtained from (ii), S2 obtained from (ii’), or S6 obtained from (iv) is fed into the second reactor at the inlet.46. The process of any one of embodiments 1 to 45, the process comprising combining S2 with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, obtaining a fifth gas stream S5, according to (iv), wherein (iv) preferably comprises combining S2 obtained from (ii) or (ii’) with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, preferably the recycle stream obtained from the second reactor as defined in embodiment 56.47. The process of any one of embodiments 1 to 46, further comprising after (ii), preferably after (ii’), and prior to (iv)(iii’) preparing a third gas stream S3, wherein S3 comprises H2, wherein S3 is preferably obtainable or obtained by a process comprising one or more of water electrolysis, NHs-reforming, preferably green NHs-reforming, steam reforming, preferably steam reforming of natural gas or bio-gas or bio-methane, and autothermal reforming of natural gas or bio-gas or bio-methane.48. The process of embodiment 47, wherein from 99 to 100 volume-%, preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of S3 prepared in (iii’) consist of H2.49. The process of embodiment 47 or 48, wherein S3 prepared in (iii’) has a volume flow rate in the range of from 10,000 to 150,000 Nm3 / h, preferably in the range of from 20,000 to 100,000 Nm3 / h, more preferably in the range of from 25,000 to 43,500 Nm3 / h, more preferably in the range of from 26,500 to 34,200 Nm3 / h.240940W001- 31 -50. The process of any one of embodiments 1 to 49, further comprising after (ii), preferably after (ii’), and prior to (iv)(iii”) preparing a fourth gas stream S4, wherein S4 comprises CO2, wherein S4 is preferably obtainable or obtained by one or more of a power plant, a steam cracker, an ammonia plant, an incineration process, a bio-process, and air, or wherein S4 is obtainable or obtained by a process comprising one or more of CO2 capture, NH3 production, hydrogen production, refining, cement production, lime production, glass production, aluminum smelting, iron smelting, and ferro-alloy production.51 . The process of embodiment 50, wherein S4 prepared in (iii”) comprises an inert gas, wherein the inert gas preferably comprises one or more of N2 and Ar, more preferably N2.52. The process of embodiment 51 , wherein S4 prepared in (iii”) comprises from 0 to 2 vol- ume-%, preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of the inert gas.53. The process of any one of embodiments 50 to 52, wherein S4 prepared in (iii”) comprises CH4, wherein S4 prepared in (iii”) comprises from 0 to 5 volume-%, preferably from 0 to 1 volume-%, more preferably from 0.1 to 0.5 volume-%, of CH4.54. The process of any one of embodiments 50 to 53, wherein from 98 to 100 volume-%, preferably from 99.5 to 100 volume-%, more preferably from 99.9 to 100 volume-%, of S4 prepared in (iii”) consist of CO2 and optionally an inert gas.55. The process of any one of embodiments 50 to 54, wherein S4 prepared in (iii”) has a volume flow rate in the range of from 1 ,000 to 50,000 Nm3 / h, preferably in the range of from 2,000 to 20,000 Nm3 / h, more preferably in the range of from 5,000 to 14,000 Nm3 / h, more preferably in the range of from 8,000 to 10,000 Nm3 / h.56. The process of any one of embodiments 1 to 55, wherein the recycle stream is obtained from the second reactor, and wherein the recycle stream comprises one or more of H2, CO, H2O, CH3OH, N2, CH4, and CO2, preferably one or more of H2, CO, and CO2.57. The process of any one of embodiments 1 to 56, wherein the recycle stream has an S value of greater than 2.30, more preferably in the range of from 2.30 to 7.00, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2) / (n(CO) + n(CO2)) (I).240940W001- 32 -58. The process of any one of embodiments 1 to 57, wherein the recycle stream, preferably the recycle stream obtained from the second reactor, more preferably the recycle stream obtained from the second reactor as defined in embodiment 56, has a volume flow rate in the range of from 10,000 to 500,000 Nm3 / h, preferably in the range of from 50,000 to 200,000 Nm3 / h, more preferably in the range of from 100,000 to 150,000 Nm3 / h, more preferably in the range of from 122,000 to 201 ,500 Nm3 / h.59. The process of any one of embodiments 1 to 58, wherein S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) is fed according to (v) into the second reactor having a volume flow rate in the range of from 5,000 to 1 ,000,000 Nm3 / h, preferably in the range of from 50,000 to 500,000 Nm3 / h, more preferably in the range of from 100,000 to 300,000 Nm3 / h, more preferably in the range of from 158,000 to 260,900 Nm3 / h.60. The process of any one of embodiments 1 to 59, wherein S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) has an S value of greater than 2.50, preferably of greater than 3.50, more preferably in the range of from 3.50 to 4.40, more preferably in the range of from 3.70 to 4.20, more preferably in the range of from 3.75 to 4.15, in the second reactor, preferably at the inlet of the second reactor, wherein the S value is calculated according to formula (II)S = (n(H2) - n(CO2) I (n(CO) + n(CO2)) (II).61 . The process of any one of embodiments 1 to 60, wherein the product stream comprises one or more of H2, CO2, and CO, preferably one or more of H2, CO2, CO, H2O, CH3OH, and one or more alkanes, more preferably one or more of H2, CO2, CO, H2O, CH3OH, dimethyl ether, formic acid, phosgene, one or more aldehydes, and one or more alkanes.62. The process of embodiment 61 , further comprising(vi) separating one or more of H2, CO2, and CO from the product stream obtained from (v), obtaining a sixth gas stream S6, wherein S6 comprises one or more of H2, CO2, and CO.63. The process of embodiment 62, further comprising after (vi)(vii) recycling at least a portion of S6 obtained from (vi) into the recycle stream according to (iv).240940W001- 33 -64. The process of any one of embodiments 1 to 63, wherein the second reactor according to (v) comprises a methanol synthesis catalyst.65. The process of embodiment 64, wherein the methanol synthesis catalyst comprised in the second reactor comprises one or more of Cu, Zn, Al, Zr, Si, and O, preferably Cu, Zn, Al, Zr, Si, and O.66. The process of embodiment 64 or 65, wherein the methanol synthesis catalyst comprised in the second reactor comprises elemental copper.67. The process of any one of embodiments 64 to 66, wherein the methanol synthesis catalyst comprised in the second reactor comprises Zn and Si, wherein the methanol synthesis catalyst comprised in the second reactor 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: 1.68. The process of any one of embodiments 64 to 67, wherein the methanol synthesis catalyst comprised in the second reactor comprises one or more oxides of Zn, Al, Zr, and Si, wherein the methanol synthesis catalyst preferably comprises one or more oxides selected from the group consisting of ZnO, ZnAhOt, and CUAI2O4, wherein more preferably the methanol synthesis catalyst comprises ZnO and ZnAhO4, or ZnO and CUAI2O4, or ZnO, ZnAhO4, and CUAI2O4.69. The process of any one of embodiments 64 to 68, wherein the methanol synthesis catalyst comprised in the second reactor 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 1.70. The process of any one of embodiments 64 to 69, wherein the methanol synthesis catalyst comprised in the second reactor comprises Cu, wherein the methanol synthesis catalyst comprised in the second reactor according to (vii) 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 determined according to Reference Example 2.71. The process of any one of embodiments 64 to 70, wherein the methanol synthesis catalyst comprised in the second reactor comprises SiC>2.240940W001- 34 -72. The process of any one of embodiments 64 to 71 , wherein the methanol synthesis catalyst comprised in the second reactor comprises Cu, Zn, Al, Zr, and Si, wherein the methanol synthesis catalyst comprised in the second reactor 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).73. The process of any one of embodiments 64 to 72, wherein from 95 to 100 weight-% of the methanol synthesis catalyst comprised in the second reactor 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-%.74. The process of any one of embodiments 1 to 74, wherein S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) fed into a second reactor are subjected in the second reactor to reaction conditions, wherein the reaction comprises one or more of a methanol synthesis, a dimethyl ether synthesis, an oxo synthesis, a Fischer-Tropsch synthesis, a formic acid synthesis, and a phosgene synthesis.75. The process of any one of embodiments 1 to 74, preferably of embodiment 74, wherein a methanol synthesis is conducted in the second reactor according to (v), and wherein the product stream comprises methanol.76. The process of embodiment 75, wherein the methanol synthesis is conducted in the second reactor according to (v) at a temperature in the range of from 190 to 280 °C, preferably in the range of from 210 to 260 °C, more preferably in the range of from 225 to 245 °C.77. The process of embodiment 75 or 76, wherein the methanol synthesis is conducted in the second reactor according to (v) at a pressure in the range of from 65 to 85 bara, preferably in the range of from 70 to 80 bara, more preferably in the range of from 73 to 77 bara.78. A process, preferably the process according to any one of embodiments 1 to 77, comprising a step of converting the product comprised in the product stream, preferably methanol, obtainable or obtained by the process according to any one of embodiments 1 to 77 to obtain a product Q.240940W001- 35 -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.Reference Example 3: SimulationsFor simulations of equilibrium gas compositions and for simulating the MeOH process, the software ASPENOPIus V11 from AspenTech was used.In the following examples, focus was on coupling the flexible rWGS process with an electrified MeOH (eMeOH) production (see also Figure 2, streams A2 and B2). For the simulations, a temperature of 870 °C and a pressure of 11 bara were set in the rWGS reactor. The H2 to CO2 ratio was 2:1 in the rWGS reactor and the rWGS reactor outlet gas stream after H2O separation had the following composition: 54.3 volume-% H2, 15.0 volume-% CO2, 29.5 volume-% CO, and 1.2 volume-% CH4). The gas composition and temperature were kept constant, only the syngas amount was varied for reflecting a flexible process (see also Figure 2, C). The syngas gas flow was varied between 500 and 15000 Nm3 / h. This additional syngas was fed into an existing eMeOH production process (see also Figure 2), wherein the CO2 inlet stream of the make-up- gas (MUG) was kept stable at 9000 Nm3 / h.As a catalyst, in particular Ni-based catalysts can be used, especially those dedicated for rWGS processes at a temperature equal to or greater than 650 °C.Comparative Example 1 : Process for preparing syngas and further processing of the syngas in methanol synthesis240940W001- 36 -Comparative Example 1 relates a scenario in which no rWGS stream was included and wherein a coupled methanol plant was run on a plant usage of 58 %. Comparative Example 1 was simulated as described in Reference Example 3. The conditions and parameters are shown in Table 1 . The MeOH process was conducted at a reactor temperature of 235 °C and a process pressure of 75 bara, wherein temperature and pressure were kept constant. The MUG consisted of H2 from water electrolysis (26430 Nm3 / h) and CO2 from, e.g., biogenic sources (9000 Nm3 / h), wherein the CO2-containing gas stream consisted of 99.5 volume-% and 0.5 volume-% N2. No syngas from the rWGS step was integrated. This resulted in a MeOH productivity of 12.45 t / d. The inert gas composition at the reactor inlet lied between 9-10 volume-%. The GHSV of 5211 h-1corresponded to a reactor size of 30 m3. The stoichiometric number S was about 4. The electricity demand noted in Table 1 related to the energy for the electrolyzer (5 kWh / Nm3) and resulted in 132150 kWh. The purge gas amount can be seen as variable and was adjusted to keep the inert in the range of 8-10 volume-%. The amount of hydrogen in the MUG can also be seen as variable and adjusted to obtain an S value of ca. 4.Example 2: Process for preparing syngas and further processing of the syngas in methanol synthesisExample 2 relates a scenario in which an rWGS stream having a comparatively low volume flow rate was used. Example 2 was simulated as described in Reference Example 3. The conditions and parameters are shown in Table 1 . The MeOH process was conducted at a reactor temperature of 235 °C and a process pressure of 75 bara, wherein temperature and pressure were kept constant. Further, the MeOH process was conducted with syngas having a comparatively low volume flow rate (500 Nm3 / h). The H2-amount in the MUG was slightly increased to reach an S value of ca. 4 and the purge increased to have a stable inert concentration. The additional syngas and hydrogen in the MUG increased also the MeOH productivity to 12.75 t / h, the GHSV to 5295 h-1and the electricity demand slightly to 136203 kWh, here additionally the energy demand for the rWGS was included.Example 3: Process for preparing syngas and further processing of the syngas in methanol synthesisExample 3 relates a scenario in which an rWGS stream having an increased volume flow rate was used compared to Example 2. Example 3 was simulated as described in Reference Example 3. The conditions and parameters are shown in Table 1. The MeOH process was conducted at a reactor temperature of 235 °C and a process pressure of 75 bara, wherein temperature and pressure were kept constant. Further, the syngas had a volume flow rate of 3600 Nm3 / h. This resulted in an increase of the MeOH productivity to 14.65 t / h, a purge of 600 Nm3 / h and a240940W001- 37 -GHSV of 6028 h-1. To keep the S value stable the H2 amount of the MUG wasincreased to 28230 Nm3 / h. Thus the electricity demand increased to 160611 kWh, here additionally the energy demand for the rWGS was included.Example 4: Process for preparing syngas and further processing of the syngas in methanol synthesisExample 4 relates a scenario in which an rWGS stream having an increased volume flow rate was used compared to Example 3. Example 4 was simulated as described in Reference Example 3. The conditions and parameters are shown in Table 1. The MeOH process was conducted at a reactor temperature of 235 °C and a process pressure of 75 bara, wherein temperature and pressure were kept constant. Further, the syngas had a volume flow rate of 8500 Nm3 / h. This resulted in an increase of the MeOH productivity to 17.65 t / h, a purge of 1000 Nm3 / h and a GHSV of 7200 IT1. To keep the S value stable the H2 amount of the MUG was increased to 30750 Nm3 / h. Thus the electricity demand increased to 199701 kWh, here additionally the energy demand for the rWGS was included.Example 5: Process for preparing syngas and further processing of the syngas in methanol synthesisExample 5 relates a scenario in which an rWGS stream having an increased volume flow rate was used compared to Example 4. Example 5 was simulated as described in Reference Example 3. The conditions and parameters are shown in Table 1. The MeOH process was conducted at a reactor temperature of 235 °C and a process pressure of 75 bara, wherein temperature and pressure were kept constant. Further, the syngas had a volume flow rate of 15000 Nm3 / h. This corresponds to an increase of the syngas by a factor 30 (compared to Example 2) This resulted in an increase of the MeOH productivity to 21.60 t / h, a purge of 1500 Nm3 / h and a GHSV of 8694 IT1. To keep the S value stable the H2 amount of the MUG was increased to 34000 Nm3 / h. Thus the electricity demand increased to 251090 kWh, here additionally the energy demand for the rWGS was included. The plant capacity or plant usage rate was set as 100 % for calculating the plant usage rate for the other examples. This means the rWGS contribution changed between Examples 2 and 5 by a factor of 30, wherein plant usage rate varied between 60 and 100%.Comparative Example 6: Process for preparing syngas and further processing of the syngas in methanol synthesis240940W001- 38 -Comparative Example 6 relates a scenario in which no rWGS stream was included and wherein a coupled methanol plant was run on a plant usage of 100 %. Comparative Example 6 was simulated as described in Reference Example 3. The conditions and parameters are shown in Table 1 . The MeOH process was conducted at a reactor temperature of 235 °C and a process pressure of 75 bara, wherein temperature and pressure were kept constant. Further, the MUG was increased by addition of CO2 (from 9000 to 15000 Nm3 / h) and H2 (from 26340 to 44000 Nm3 / h) to reach the same process parameters as in Example 5. Due to the slightly different gas compositions, the purge was comparatively small (750 Nm3 / h). The other key parameters were as similar as possible compared to Example 5.Example 7: Overview of conditions and parameters for Comparative Example 1, Examples 2-5, and Comparative Example 6, and discussion of resultsIn Table 1 , conditions and parameters are noted for Comparative Example 1 reflecting the scenario in which no rWGS stream was included and wherein methanol plant was run on a plant usage of 58 %, Examples 2-5 reflecting scenarios with varied volume flow rate of the rWGS stream, and Comparative Example 6 reflecting the scenario in which no rWGS stream was included and wherein methanol plant was run on a plant usage of 100 %.Tablel240940W001- 39 -As can be gathered from the results shown in Table 1 , the coupling of the rWGS and the eMeOH enables not only a higher electricity demand, thus an enlarged participation in stabilizing the electric grid, but also allows coupling the dynamic electric grid to a flexible rWGS process, thereby avoiding direct influence of the fluctuating character of the hydrogen supply on the MeOH production.DESCRIPTION OF FIGURESFigure 1 : illustrates the general concept of the process of the present invention, wherein an rWGS process is combined with a further chemical process. In particular, H2 from regenerative sources (stream-A) and CO2, e.g., from bio-sources (stream-B) are fed into an electrified rWGS reactor (C). The reactor outlet can then be used for various applications like syngas (stream-D), oxo-gas (stream-E) or as CO-point source (stream-F).Figure 2: illustrates a specific embodiment of the process of the present invention, wherein an rWGS process is combined with methanol production. In particular, H2 from regenerative sources (stream-A1) and CO2, e.g., from bio-sources (stream-B1) are fed into an electrified rWGS reactor (C). The reactor outlet can then be combined with H2 from regenerative sources (stream-A2) and CO2, e.g., from bio-sources (stream-B2) in a methanol production (D), thereby generating an additional methanol capacity (E).CITED LITERATURE- WO 2023 / 41396 A1- WO 2008 / 115933 A1- WO 2021 / 062384 A1C. Markowitsch et al. “Impact of the operation conditions on the reverse-water-gas shift reaction” in Global Challenges for a Sustainable Society: EURECA-PRO the European University for Responsible Consumption and Production 2023240940W001-40 -- US 2024 / 002221 A1

Claims

1. 240940W001- 41 -Claims1 . A process for preparing and processing of synthesis gas, the process comprising(i) preparing a first gas stream S1 , wherein S1 comprises H2 and CO2, wherein S1 has a H2:CC>2 molar ratio in the range of from 0.5:1 to 4:1 ;(ii) feeding S1 prepared in (i) into a first reactor comprising a reverse water gas shift catalyst, wherein S1 is fed into the first reactor at a gas hourly space velocity (GHSV) in the range of from 1 ,000 to 100,000 h’1, wherein the reverse water gas shift reaction is conducted at a temperature in the range of from 650 to 1 ,000 °C, wherein in a time interval At, wherein At is in the range of from 1 to 60 minutes, the GHSV of S1 displays a gradient in the range of from 2,000 to 60,000 h’1, obtaining a second gas stream S2, wherein S2 comprises CO, H2, CO2, and optionally H2O;(iii) optionally separating one or more of H2O, CO2, CH4 and H2 from S2;(iv) optionally combining S2 with one or more of a third gas stream S3, wherein S3 comprises H2, a fourth gas stream S4, wherein S4 comprises CO2, and a recycle stream, obtaining a fifth gas stream S5;(v) feeding S2 obtained from (ii), S2 obtained from (iii), or S5 obtained from (iv) into a second reactor, wherein the second reactor comprises one or more of a methanol synthesis catalyst, a dimethyl ether synthesis catalyst, an oxo synthesis or hydroformylation catalyst, a Fischer-Tropsch synthesis catalyst, a formic acid synthesis catalyst, and a phosgene synthesis catalyst, obtaining a product stream.

2. The process of claim 1 , wherein preparing S1 according to (i) comprises combining a H2- containing stream and a CO2-containing stream.

3. The process of claim 1 or 2, wherein the first reactor according to (ii) is electrically heated.

4. The process of any one of claims 1 to 3, wherein the reverse water gas shift catalyst comprised in the first reactor according to (ii) comprises Ni.

5. The process of any one of claims 1 to 4, wherein the reverse water gas shift reaction is conducted according to (ii) at a pressure in the range of from 2 to 25 bara.

6. The process of any one of claims 1 to 5, wherein during the time interval At in (ii), the reaction temperature is maintained between a maximum temperature Tmax and a minimum temperature Tmin, wherein AT = Tmax - Tmin is in the range of from 0 to 25 K.240940W001- 42 -7. The process of any one of claims 1 to 6, wherein S2 obtained from (ii) further comprises H2O, and wherein the process further comprises after (ii) and prior to (iii), (iv) or (v)(ii’) Separating at least a portion of H2O from S2 obtained from (ii).

8. The process of any one of claims 1 to 7, wherein S2 obtained from (ii) or (ii’) comprises from 23.0 to 36.0 volume-% of CO.

9. The process of any one of claims 1 to 8, wherein S2 obtained from (ii) or (ii’) comprises from 44.0 to 65.0 volume-% of H2.

10. The process of any one of claims 1 to 9, wherein S2 obtained from (ii) or (ii’) comprises from 10.0 to 20.0 volume-% of CO2.

11. The process of any one of claims 1 to 10, wherein the recycle stream is obtained from the second reactor, and wherein the recycle stream comprises one or more of H2, CO, and CO2.

12. The process of any one of claims 1 to 11 , wherein the recycle stream has an S value of greater than 2.30, wherein the S value is calculated according to formula (I)S = (n(H2) - n(CO2) I (n(CO) + n(CO2)) (I).

13. The process of any one of claims 1 to 12, wherein S2 obtained from (ii), S2 obtained from (ii’), S2 obtained from (iii), or S5 obtained from (iv) has an S value of greater than 2.50 in the second reactor, wherein the S value is calculated according to formula (II)S = (n(H2) - n(CO2) I (n(CO) + n(CO2)) (II).

14. The process of any one of claims 1 to 13, wherein the product stream comprises one or more of H2, CO2, CO, H2O, CH3OH, dimethyl ether, formic acid, phosgene, one or more aldehydes, and one or more alkanes.

15. A process comprising a step of converting the product comprised in the product stream obtainable or obtained by the process according to any one of claims 1 to 14 to obtain a product Q.

Images