Co-production of acrylic acid, acrylic acid derivatives, ethylene oxide, and olefins

Abstract

The present invention relates to a process for co-producing acrylic acid and / or acrylic acid deriv- atives, preferably parallel to the production of ethylene oxide and / or a product of a cracking re- action, wherein at least part or all of the carbon dioxide required for co-producing acrylic acid and / or acrylic acid derivatives originates from the production of ethylene oxide and / or olefins, as well as to the use of said process for co-producing acrylic acid and / or acrylic acid derivatives.

Description

240823W001Co-production of acrylic acid, acrylic acid derivatives, ethylene oxide, and olefinsTECHNICAL FIELDThe present invention relates to a process for co-producing acrylic acid and / or acrylic acid derivatives parallel to the production of ethylene oxide and / or a product of a cracking reaction, as well as to the use of thereof for co-producing acrylic acid and / or acrylic acid derivatives.INTRODUCTIONAcrylic acid and its derivatives constitute highly important building blocks for many industrial and consumer products, such as coatings, textiles, adhesives, paints, plastics, as well as in medicine and dentistry. The total worldwide productivity of acrylic acid alone is more than six million tons per year. However, with increasingly strict standards with regard to carbon dioxide emissions and the endeavor to provide increasingly economic and environmental-friendly methods, the classical industrial syntheses of acrylic acid, for example the most common two-step oxidation of propene with oxygen, are not ideal to achieve the desired economic production process. A promising alternative to provide such a production process for acrylic acids with a reduced carbon footprint would be the direct reaction of the cheap and abundant starting materials carbon dioxide and ethylene. In particular, by employing carbon dioxide that stems from processes running in parallel to the production of acrylic acids, the carbon footprint of the overall manufacturing plant could possibly be reduced.X. Wang, H. Wang, and Y. Sun, “Synthesis of Acrylic Acid Derivatives from CO2 and Ethylene,” Chem, vol. 3, no. 2, pp. 211-228, Aug. 2017 describes an overview of research dedicated to the direct functionalization of alkenes, in particular ethylene, with the use of carbon dioxide as the carboxylation reagent, wherein general principles as well as more detailed insights into catalyst designs and reaction mechanisms are discussed.M. Zhang and Y. Yu, “Dehydration of Ethanol to Ethylene,” Ind. Eng. Chem. Res., vol. 52, no.28, pp. 9505-9514, Jul. 2013, discloses an up-to-date review on the dehydration of ethanol to ethylene with regard to the production process, catalysts and reaction mechanisms.A. M. Bahmanpour, M. Signorile, and O. Krbcher, “Recent progress in syngas production via catalytic CO2 hydrogenation reaction,” Applied Catalysis B: Environmental, vol. 295, p. 120319,240823W001- 2 - Oct. 2021 discloses recent progress in the production of synthesis gas through the catalytic reverse water-gas shift reaction as an attractive option for the conversion of carbon dioxide to fuels, and highlights developments in catalyst design and the understanding of reaction pathways.S. S. Ali, S. S. Ali, and N. Tabassum, “A review on CO2 hydrogenation to ethanol: Reaction mechanism and experimental studies,” Journal of Environmental Chemical Engineering, vol. 10, no. 1, p. 106962, Feb. 2022, discusses the carbon dioxide hydrogenation to ethanol as a means to lower carbon dioxide emissions by transforming the carbon dioxide into valuable fuel, and focuses on the study of reaction mechanisms and experimental investigation.L. Petrescu, M. Fermeglia, and C.-C. Cormos, “Life Cycle Analysis applied to acrylic acid production process with different fuels for steam generation,” Journal of Cleaner Production, vol. 133, pp. 294-303, Oct. 2016, discloses a life cycle analysis to determine the environmental impact of the acrylic acid production using propylene as a raw material, thereby taking into consideration the different phases, namely extraction, processing, transport, manufacturing, distribution, and usage of the obtained products.P. Tian, Y. Wei, M. Ye, and Z. Liu, “Methanol to Olefins (MTO): From Fundamentals to Commercialization,” ACS Catal., vol. 5, no. 3, pp. 1922-1938, Mar. 2015, provides a historical perspective on the key issues for the process development, including studies on the reaction mechanism, molecular sieve synthesis and crystallization mechanism, catalyst and its manufacturing scale-up, reactor selection and reactor scale-up, process demonstration, and commercialization of the methanol-to-olefins reaction.X. Jiang et al., “Recent Advances in Carbon Dioxide Hydrogenation to Methanol via Heterogeneous Catalysis”, Chem. Rev., vol. 120, no. 15, pp. 7984-8034, Feb. 2020, describes a comprehensive overview on recent advances in the hydrogenation of carbon dioxide to methanol via heterogeneous catalysis, thereby focusing on the catalyst design and development, and theoretical studies of the reaction mechanism.S. Nitopi et al., “Progress and Perspectives of Electrochemical CO2 Reduction on Copper in Aqueous Electrolyte,” Chem. Rev., vol. 119, no. 12, pp. 7610-7672, Jun. 2019, discusses the electrochemical carbon dioxide reduction using copper in an aqueous electrolyte, in particular with regard to the variety of factors that impact activity, selectivity, including the catalyst surface structure, morphology, composition, the choice of electrolyte ions and pH, and the electrochemical cell design.240823W001- 3 - K. Wiranarongkorn, K. Eamsiri, Y.-S. Chen, A. Arpornwichanop, “A comprehensive review of electrochemical reduction of CO2 to methanol: Technical and design aspects” J. CO2 Util., vol.71, 102477, May 2023, describes present progress of the development of electrochemical CO2 reduction technology for methanol production with regard to both experimental studies, particularly electro-catalyst design and development, and process design and analysis to overcome challenges such as low CO2 solubility, low product selectivity, inefficient catalysts, mass transfer limitations, high overpotentials, and technology commercialization.X. Cui, S. K. Kaer, “A comparative study on three reactor types for methanol synthesis from syngas and CO2”, Chem. Eng. J., vol. 393, article 124632, Aug. 2020, discloses a comparative study on the three reactor types employed for the traditional syngas to methanol process, wherein the reactor types are a adiabatic reactor, a water-cooled reactor, and a gas-cooled reactor.Y. Mao et al., “Progress in the thermo-catalytic hydrogenation of CO2 to ethanol”, J. Fuel Chem. Technol., vol 51, no. 10, pp. 1514-1528, Oct. 2023, describes the research progress made in the thermo-catalytic hydrogenation of CO2 to ethanol with regard to the performance of various catalysts, support materials and its synergistic effects on the CO2 conversion. Further, appropriate conditions as well as possible reaction mechanism for the CO2 hydrogenation to ethanol are discussed.A. I. Latsiou et al., “CO2 hydrogenation for the production of higher alcohols: Trends in catalyst developments, challenges and opportunities”, Catalysis today, vol. 420, article 114179, Aug. 2023, discloses a comprehensive and critical review of the catalytic formulations that are employed, in both fixed-bed and batch reactors, which include noble metal catalysts, transition metal-based systems, post-transition metal catalysts, bimetallic, multimetallic / multi-functional catalysts, Metal Organic Frameworks (MOFs), perovskite-, and zeolite-based catalysts. Further, the impact of promoters, supports and reaction conditions as well as insights into mechanistic details are also discussed.T. Lu et al., “Electrocatalytic CO2 Reduction to Ethylene: From Advanced Catalyst Design to Industrial Applications”, Adv. Mater., vol. 35, article 202310433, Nov. 2023 relates to the catalyst design strategies, in particular with regard to morphology, crystallinity, oxidation state, defects, composition, and surface engineering, for the electrochemical CO2 reduction reaction as well as the industrial implementation of these catalysts for the production of ethylene with highlights on the key strategies and comprehension of recent advancements, remaining challenges and future directions.240823W001-4 - I. Jang et al., “Electrocatalysis in Solid Oxide Fuel Cells and Electrolyzers”, Chem. Rev., vol. 124, pp. 8233-8306, June 2024 discloses a review over solid oxide electrochemical cells with regard to the diverse range of electrocatalytic materials used therein, their electrochemical activity, evaluation of electrochemical performance, catalyst design and catalyst deactivation mechanisms.R. Chauhan et al., “Advancements in Environmentally Sustainable Technologies for Ethylene Production”, Energy Fuels, vol. 37, pp. 12589-12622, Aug. 2023 provides an overview of the performance attributes of conventional reactors and the crucial features of electrochemical reactors and examines the economic aspects of “green ethylene” production.WO 2019 / 053540 A1 relates to a method of producing an alkali metal or alkaline earth meal acrylate, wherein the method comprises reacting ethylene and carbon dioxide with a composition comprising a carboxylation catalyst, preferably a transition metal catalyst, and a base. The carbon dioxide may be obtained from a waste or recycle gas stream or after recovering the carbon dioxide from a gas stream.WO 2024 / 132696 A1 relates to a process for converting biomass into acrylate salts, wherein said process comprises (a) a treatment of biomass to produce ethanol and carbon dioxide, (b) a dehydration of the ethanol to obtain ethylene, and (c) a synthesis of acrylate salts from ethylene and carbon dioxide in the presence of a catalytic precursor and a solvent.US 2011 / 112314 A1 relates to a process for producing olefins, wherein said process comprises the cracking of an ethane-comprising feed to obtain a cracking-zone effluent comprising olefins, in particular ethylene, as well as the conversion of an oxygenate feedstock to obtain an oxygen-to-olefin zone effluent comprising olefins. The oxygenate feed is thereby produced by reacting hydrogen with carbon monoxide and / or carbon dioxide, wherein in particular the carbon dioxide may be obtained from a carbon dioxide comprising flue gas stream, preferably from an oxidative de-coking of an ethane cracking furnace.WO 03 / 055869 A1 relates to the purification of ethylene oxide, wherein the ethylene oxide is obtained by the gas-phase catalytic oxidation of ethylene by molecular oxygen. The gas stream received as a by-product in the synthesis of the ethylene oxide may then be decarbonized in an absorption column to recycle a gas stream that is at least partially freed from carbon dioxide, which is then fed back to the ethylene oxide synthesis.Despite the progress made, the direct reaction of ethylene and carbon dioxide to produce acrylic acid derivatives and the significant advantages associated therewith, such as potential240823W001- 5 -recycling of carbon dioxide from parallel processes, remain underutilized in the industrial context, which, however, create a need for new and improved manufacturing processes for the greener production of acrylic acid derivatives and other valuable feedstocks.DETAILED DESCRIPTIONThus, it was an object of the present invention to provide an economically and environmentally attractive production of acrylic acids and its derivatives, of ethylene oxides and of olefins.It was surprisingly found that by employing carbon dioxide originating from the production of ethylene oxide and / or from a cracking plant in a reaction with ethylene to produce acrylic acid and its derivatives, the carbon footprint of the produced acrylic acid and its derivatives, the ethylene oxide as well as of the olefins obtained in the cracking plant can be reduced. Additionally, it was surprisingly found that by synthesizing the ethylene from bioethanol, from syngas obtained from the same source of carbon dioxide, and / or by hydrogenation or electrochemical reduction of said carbon dioxide, the carbon footprint of the manufactured products can be further reduced.Therefore, the present invention relates to a process for co-producing acrylic acid and / or acrylic acid derivatives, preferably parallel to the production of ethylene oxide and / or a product of a cracking reaction, comprising(i) preparing a stream Sc comprising carbon dioxide;(ii) preparing a stream SE comprising ethylene;(iii) reacting at least part or all of the stream Sc and at least part or all, preferably all, of the stream SE in the presence of a catalyst CA, obtaining a product stream P comprising acrylic acid, an acrylic acid derivative, or acrylic acid and an acrylic acid derivative;wherein at least part or all of the CO2 comprised in the stream Sc is obtained as a by-product from a reaction of ethylene and oxygen to produce ethylene oxide, and / or wherein at least part or all of the CO2 comprised in the stream Sc is obtained from a flue gas stream from combustion of a carbonaceous fuel to produce heat for a cracking reaction.It is preferred that the process is a continuous process.As a first alternative, it is preferred that (ii) comprises(ii.A) converting a part of the stream Sc comprising CO2 by hydrogenation or by electrochemical reduction of CO2 contained in said part of the Stream Sc, obtaining a stream SPI240823W001- 6 - comprising ethanol, or ethylene and ethanol;(ii.B) converting at least part or all, more preferably all, of the ethanol comprised in the stream SPI to ethylene in the presence of a dehydration catalyst CD, obtaining a stream SP2 comprising ethylene.In the case where (ii) comprises (ii.A) and (ii.B), it is preferred that the hydrogenation in (ii.A) comprises reacting the stream Sc in the presence of a hydrogenation catalyst CH, H2, and optionally a solvent.In the case where the hydrogenation in (ii.A) comprises reacting the stream Sc in the presence of a hydrogenation catalyst CH, H2, and optionally a solvent, it is preferred that the catalyst CH comprises a metal selected from the group consisting of Al, Ti, Fe, Co, Ni, Cu, Mo, Ru, Rh, Pd, Ag, Ir Pt, Au, La, Ce, Ga, Zr, and mixtures of two or more thereof.Further in the case where the hydrogenation in (ii.A) comprises reacting the stream Sc in the presence of a hydrogenation catalyst CH, H2, and optionally a solvent, it is preferred that the hydrogenation in (ii.A) is conducted at a temperature in the range of from 50 to 1000 °C, more preferably in the range of from 200 to 900 °C, more preferably in the range of from 350 to 850 °C.In the case where (ii) comprises (ii.A) and (ii.B), it is preferred that the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of a cathode and an anode, wherein the cathode comprises C, Cu, Ag, Zn, Sn, In, Ga, Au or mixtures of two or more thereof,wherein the anode comprises C, Ir, Ru, Pt, Ni, Co, La, Sr, Fe Fe, or mixtures of two or more thereof.In the case where the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of a cathode and an anode, it is preferred that the cathode comprises Cu, wherein the cathode is selected from the group consisting of pure Cu, nanostructured Cu, Cu nanoparticles, oxidized Cu, Cu foams, doped Cu, Cu alloys such as Cu-Ag, Cu-Zn, or Cu-Sn, bimetallic catalysts such as Cu-ln, Cu-Ga, or Cu-Au, core-shell catalysts, carbon-based hybrid materials such as Cu-graphene / graphite or Cu-carbon nanotubes, Cu phosphides, Cu-based metal-organic frameworks, and mixtures of two or more thereof.In the case where the cathode comprises Cu alloys, it is preferred that the Cu alloys are selected from the group consisting of Cu-Ag, Cu-Zn, Cu-Sn, and mixtures of two or more thereof.240823W001- 7 - In the case where the cathode comprises bimetallic catalysts, it is preferred that the bimetallic catalysts are selected from the group consisting of Cu-ln, Cu-Ga, Cu-Au, and mixtures of two or more thereof.In the case where the cathode comprises carbon-based hybrid materials, it is preferred that the carbon-based hybrid materials are selected from the group consisting of Cu-graphene, Cu-graphite, Cu-carbon nanotubes, and mixtures of two or more thereof.Further in the case where the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of a cathode and an anode, it is preferred that the anode is selected from the group consisting of Ir-oxide, Ru-oxide, Ni foam, Ni-oxide, Ni-hydroxide, Ni-Fe alloy, Ni-Fe-oxide, Co-oxide, Co-Fe alloy, perovskite oxides, Pt, carbon-based materials such as doped graphene, carbon nanotubes, or hybrid composite supports, and mixtures of two or more thereof.In the case where the anode comprises carbon-based materials, it is preferred that the carbonbased hybrid materials are selected from the group consisting of Cu-graphene, Cu-graphite, Cu-carbon nanotubes, and mixtures of two or more thereof.Further in the case where the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of a cathode and an anode comprise a dopant, wherein the dopant is more preferably selected from the group consisting of Ca, V, Ti, Fe, Co, Ni, Cu, Nd, Hf, Eu, and mixtures of two or more thereof.Further in the case where the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of a cathode and an anode, it is preferred that the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of an electro-catalyst CE.In the case where the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of an electro-catalyst CE, it is preferred that the catalyst CE is selected from the group consisting of metals, metal oxides, metal complexes, metal organic frameworks, metal-free electro-catalysts, and mixtures of two or more thereof.In the case where the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of an electro-catalyst CE, it is preferred that the catalyst CE is coated on the cathode or the anode.Further in the case where (ii) comprises (ii.A) and (ii.B), it is preferred that the process after (ii.A) and prior to (ii.B) comprises(ii.S.1) independently from each other separating ethylene and ethanol from thestream SPI, obtaining at least part or all of the stream SE, a stream comprising240823W001- 8 - ethanol, and a stream SPI depleted of ethylene and ethanol;(U.S.2) feeding the stream comprising ethanol obtained in (ii.S.1) into step (ii.B).Further in the case where (ii) comprises (ii.A) and (ii.B), it is preferred that the catalyst CD in (ii.B) comprises an oxidic material, wherein more preferably the oxidic material is selected from the group consisting of a metal oxide, a molecular sieve, a heteropolyacid, and mixtures of two or more thereof.Further in the case where (ii) comprises (ii.A) and (ii.B), it is preferred that the process after (ii.B) further comprises a step of separating ethylene from the stream Sp2to obtain at least part or all of the stream SE.As a second alternative, it is preferred that (ii) comprises(ii.A) converting a part of the stream Sc comprising CO2 by hydrogenation or by electrochemical reduction of CO2 contained in said part of the Stream Sc, obtaining a stream SPI comprising ethylene.In the case where (ii) comprises (ii.A), it is preferred that the process after (ii.A) further comprises a step of separating ethylene from the stream SPI to obtain at least part or all of the stream SE.As a third alternative, it is preferred that (ii) comprises(ii.a) preparing a stream SOH comprising an alcohol;(ii.b) converting at least part or all, more preferably all, of the stream SOH, obtaining a stream So comprising ethylene, propylene, or ethylene and propylene(ii.c) separating ethylene from the stream So, obtaining at least part or all of the stream SE and a stream So depleted of ethylene.In the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that the alcohol of the stream SOH is selected from the group consisting of methanol, ethanol, 1 -propanol, 2-propanol ,1 -butanol, 2-butanol, 1-pentanol, 1-hexanol, 1-heptanol, and mixtures of two or more thereof, more preferably from the group consisting of methanol and ethanol, wherein more preferably the alcohol of the stream SOH comprises, more preferably consists of, ethanol.Further in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that (ii.a) comprises (ii.a.1) preparing a stream SH comprising H2;(ii.a.2) reacting at least part of the stream Sc with at least part or all of the streamSH in the presence of a gas shift catalyst CGS, obtaining a stream Sscomprising H2 and CO;240823W001- 9 - (ii.a.3) converting at least part or all, more preferably all, of the stream Ss in the presence of an alcohol formation catalyst COH, obtaining the stream SOH.In the case where (ii.a) comprises (ii.a.1), (ii.a.2) and (ii.a.3), it is preferred that the reaction in step (ii.a.2) is a reverse water gas shift reaction, wherein the following reaction occurs:CO2+ H2CO + H2OFurther in the case where (ii.a) comprises (ii.a.1), (ii.a.2) and (ii.a.3), it is preferred that the catalyst CGS in step (ii.a.2) comprises a metal selected from the group consisting of Ni, Co, Fe Cu, Zn, Mn, Pd, Pt, Rh, Zr, In, Ga, La, Ce, and mixtures of two or more thereof.Further in the case where (ii.a) comprises (ii.a.1), (ii.a.2) and (ii.a.3), it is preferred that converting the stream Ss in step (ii.a.3) comprises reacting said stream with a part of the stream SH in the presence of the catalyst COH.Further in the case where (ii.a) comprises (ii.a.1), (ii.a.2) and (ii.a.3), it is preferred that the catalyst COH in step (ii.a.3) comprises a metal selected from the group consisting of Fe, Co, Cu, Zn, Mo, Ru, Rh, Pd, Pt, Au, and mixtures of two or more thereof.Further in the case where (ii.a) comprises (ii.a.1), (ii.a.2) and (ii.a.3), it is preferred that the alcohol comprised in the stream SOH obtained in step (ii.a.3) is ethanol and one or more of 1 -propanol, 2-propanol, 1-butanol, 2-butanol, and 2-methyl-1 -propanol, more preferably one or more of 1-butanol, 2-butanol and 2-methyl-1 -propanol.Further in the case where (ii.a) comprises (ii.a.1), (ii.a.2) and (ii.a.3), it is preferred that the catalyst CGS and the catalyst COH are the same catalyst.Alternatively, in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that (ii.a) comprises a fermentation of glucose, obtaining the stream SOH comprising, more preferably consisting of, ethanol, wherein at least part of the CO2 comprised in the stream Sc is further obtained as a by-product.Further in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that SOH comprises, more preferably consists of, ethanol, wherein (ii.b) comprises converting at least part or all of the stream SOH in the presence of a dehydration catalyst CD, obtaining the stream So comprising ethylene240823W001- 10 - In the case where (ii.b) comprises converting at least part or all of the stream SOH in the presence of a dehydration catalyst CD, it is preferred that the catalyst CD comprises an oxidic material, wherein more preferably the oxidic material is selected from the group consisting of a metal oxide, a molecular sieve, a heteropolyacid, and mixtures of two or more thereof.Further in the case where (ii.b) comprises converting at least part or all of the stream SOH in the presence of a dehydration catalyst CD, it is preferred that the step (ii.b) is conducted at a temperature in the range of from 100 to 800 °C, more preferably in the range of from 200 to 600 °C, more preferably in the range of from 300 to 500 °C.Further in the case where (ii.b) comprises converting at least part or all of the stream SOH in the presence of a dehydration catalyst CD, it is preferred that the step (ii.b) is conducted at a pressure in the range of from 0.1 to 20 bar(abs), more preferably in the range of from 0.5 to 10 bar(abs), more preferably in the range of from 1 to 2 bar(abs).Further in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that SOH comprises, more preferably consists of, ethanol and wherein only part of the stream SOH is converted in step (ii.b), wherein the process further comprises(iv) converting at least part or all, more preferably all, of the stream SOH that is not employed in step (ii.b) in the presence of one or more catalysts, obtaining a stream SP comprising propylene.As a first alternative, in the case where the process further comprises (iv), it is preferred that step (iv) comprises(iv.1 ) converting the stream SOH in the presence of the dehydration catalyst CD, obtaining a stream comprising ethylene;(iv.2) converting the stream comprising ethylene in the presence of one or more catalysts, obtaining the stream SP comprising propylene.In the case where step (iv) comprises (iv.1) and (iv.2), it is preferred that converting in step (iv.2) is performed in the presence of a oligomerization catalyst CEP.In the case where converting in step (iv.2) is performed in the presence of a oligomerization catalyst CEP, it is preferred that the catalyst CD and the catalyst CEP are the same catalyst.Alternatively, in the case where step (iv) comprises (iv.1 ) and (iv.2), it is preferred that step (iv.2) comprises(iv.2.1) converting the stream comprising ethylene in the presence of a dimerization catalyst CDM, obtaining a stream comprising 2-butene;240823W001- 11 - (iv.2.11) converting the stream comprising 2-butene in the presence of a metathesis catalyst CM, obtaining the stream SP comprising propylene.In the case where step (iv.2) comprises (iv.2.1) and (iv.2. II), it is preferred that the catalyst CDM and the catalyst CM are the same catalyst.In the case where step (iv.2) comprises (iv.2.1) and (iv.2. II), it is preferred that the catalysts CD, CDM and CM are the same catalyst.Alternatively, in the case where step (iv) comprises (iv.1) and (iv.2), step (iv.2) comprises (iv.2.1’) converting the stream comprising ethylene in the presence of a trimerization catalyst CTM, obtaining a stream comprising 1 -hexene;(iv.2. II’) converting the stream comprising 1-hexene in the presence of a p-fission catalyst CBF, obtaining the stream SP comprising propylene.In the case where step (iv.2) comprises (iv.2.1’) and (iv.2. II’), it is preferred that the catalyst CTM and the catalyst CBF are the same catalyst.Further in the case where step (iv.2) comprises (iv.2.1’) and (iv.2. II’), it is preferred that the catalysts CD, CTM and CBF are the same catalyst.Further in the case where step (iv) comprises (iv.1 ) and (iv.2), it is preferred that the catalysts CD, CEP, CDM, CM, CTM and CBF comprise acidic active sites.In the case where the catalysts CD, CEP, CDM, CM, CTM and CBF comprise acidic active sites, it is preferred that the catalysts CD, CEP. COM, CM, and CBF comprise a zeolitic material having a framework structure type selected from the group consisting of AEI, BEA, ERI, EUO, FAU, FER, GIS, HEU, LTA, LTL, MFI, MOR, MTW, MWW, RHO, and mixtures of two or more thereof, more preferably AEI, BEA, CHA or MFI, more preferably MFI.In the case where the catalysts CD, CEP. COM, CM, and CBF comprise a zeolitic material, it is preferred that the zeolitic material further comprises a metal selected from the group consisting of Mg, Ca, Ba, Sr, Fe, Cr, Ce, Co, Cu, Ni, Zr, Mo, Ag, Au, W, La, Pd, Pt, Ru, Rh, Re, Ir, and mixtures of two or more thereof.As a second alternative, in the case where the process further comprises (iv), it is preferred that step (iv) comprises(iv.T) converting a part of the stream SOH in the presence of a dehydrogenate catalyst CEA, obtaining a stream comprising acetaldehyde;(iv.2’) converting the stream comprising acetaldehyde in the presence of a ketonization catalyst CAA, obtaining a stream comprising acetone;240823W001- 12 - (iv.3’) converting the stream comprising acetone in the presence of a hydrogenationdehydration catalyst CAP, obtaining the stream SP comprising propylene.In the case where step (iv) comprises (iv.T), (iv.2’) and (iv.3’), it is preferred that the catalysts CEA, CAA and CAP are the same catalyst.Further in the case where step (iv) comprises (iv.1 ’), (iv.2’) and (iv.3’), it is preferred that the catalysts CEA, CAA and CAP comprise basic active sites.In the case where the catalysts CEA, CAA and CAP comprise basic active sites, it is preferred that the catalysts CEA, CAA and CAP comprise a metal oxide.In the case where that the catalysts CEA, CAA and CAP comprise a metal oxide, it is preferred that the metal in the metal oxide is selected from the group consisting of Y, Ce, Zr, In, and mixtures of two or more thereof.Further in the case where that the catalysts CEA, CAA and CAP comprise a metal oxide, it is preferred that the catalysts CEA, CAA and CAP further comprise a zeolitic material.In the case where the catalysts CEA, CAA and CAP further comprise a zeolitic material, it is preferred that the zeolitic material has framework structure type selected from the group consisting of AEI, BEA, ERI, EUO, FAU, FER, GIS, HEU, LTA, LTL, MFI, MOR, MTW, MWW, RHO, and mixtures of two or more thereof, more preferably AEI, BEA, CHA or MFI, more preferably BEA.Alternatively, in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that (ii.a) comprises converting a part of the stream Sc by hydrogenation or by electrochemical reduction, obtaining the stream SOH comprising methanol.Further in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that (ii.b) comprises (ii.b. I) converting at least part or all, more preferably all, of the stream SOH in in the presence of a methanol-to-olefin catalyst Cmto, obtaining the stream So comprising ethylene and propylene;(ii.b. II) separating ethylene from the stream So, obtaining at least part or all of the stream SE and a stream So depleted of ethylene.In the case where (ii.b) comprises (ii.b. I) and (ii.b. II), it is preferred that (ii.b) further comprises (ii.b. Ill) separating propylene from the stream So depleted of ethylene, obtaining the stream SP.240823W001- 13 - Further in the case where (ii.b) comprises (ii.b.l) and (ii.b.ll), it is preferred that the catalyst Cmto comprises a zeolitic material having a framework structure type selected from the group consisting of AEI, BEA, ERI, EUO, FAU, FER, GIS, HEU, LTA, LTL, MFI, MOR, MTW, MWW, RHO, or mixtures of two or more thereof, more preferably AEI, BEA, CHA or MFI, more preferably CHA.In the case where the catalyst Cmto comprises a zeolitic material, it is preferred that the zeolitic material comprises H-beta, ZSM-22, ZSM-5 and / or SAPO-34.Further in the case where (ii.b) comprises (ii.b.l) and (ii.b.ll), it is preferred that the step (ii.b.l) is conducted at a temperature in the range of from 100 to 1000 °C, more preferably in the range of from 200 to 800 °C, more preferably in the range of from 350 to 600 °C.Further in the case where (ii.b) comprises (ii.b.l) and (ii.b.ll), it is preferred that the step (ii.b.l) is conducted at a pressure in the range of from 0.1 to 20 bar(abs), more preferably in the range of from 0.5 to 10 bar(abs), more preferably in the range of from 1 to 3 bar(abs)Further in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that propylene is comprised in the stream So or the stream SP is obtained, wherein the process further comprises (v) converting at least part or all of the propylene comprised in the stream So orthe stream SP in the presence of oxygen and an oxidation catalyst Co, obtaining a product stream PA comprising acrylic acid.Further in the case where (ii) comprises (ii.a), (ii.b) and (ii.c), it is preferred that propylene is comprised in the stream So or the stream Spis obtained, wherein the process further comprises (v’) converting at least part or all of the propylene comprised in the stream So orthe stream SP in the presence of a hydroformylation catalyst CB, obtaining a stream SB comprising butanol;(vi’) converting at least part or all of the stream SB, obtaining a product stream PB comprising butyl acrylate.In the case where the process further comprises (v’) and (vi’), it is preferred that converting in the step (v’) comprises the steps of a hydroformylation and a hydrogenation.In the case where the step (v’) comprises the steps of a hydroformylation and a hydrogenation, it is preferred that the catalyst CB is present in the hydroformylation step.Further in the case where the process further comprises (v’) and (vi’), it is preferred that the step (vi’) comprises reacting at least part or all of the stream SB with acrylic acid or an acrylic acid derivative.240823W001- 14 - It is preferred that the catalyst CA in step (iii) comprises a metal complex comprising a metal MA and a ligand LA.In the case where step (iii) comprises a metal complex comprising a metal MA and a ligand LA, it is preferred that the metal MA is selected from the group consisting of Fe, Ni, Co, Mo, Pd, Ru, Rh, Ir, Pt, W, Ag, Au, and mixtures of two or more thereof.Further in the case where step (iii) comprises a metal complex comprising a metal MA and a ligand LA, it is preferred that the ligand LA is selected from the group consisting of amine ligands, phosphine ligands, olefin ligands, and mixtures of two or more thereof.It is preferred that reacting in step (iii) is carried out in the the presence of a base.It is preferred that reacting in step (iii) is carried out in the presence of a solvent.It is preferred that reacting in step (iii) is carried out in the presence of a reductant and / or an alkylation agent.It is preferred that the reacting in step (iii) is conducted at a temperature in the range of from 25 to 1200 °C, more preferably in the range of from 100 to 800 °C, more preferably in the range of from 200 to 500 °C.It is preferred that the reacting in step (iii) is conducted at a pressure in the range of from 0.1 to 400 bar(abs), more preferably in the range of from 10 to 200 bar(abs), more preferably in the range from 50 to 150 bar(abs).It is preferred that the acrylic acid derivative comprise the general formula (A)wherein X is N, O, or S;wherein R is H, Li, Na, K, Cs or C1-C4-alkyl.In the case where the acrylic acid derivative comprises the general formula (A), it is preferred that the acrylic acid derivative is selected from the group consisting of lithium acrylate, sodium acrylate, methyl acrylate, ethyl acrylate, and mixtures of two or more thereof, wherein more preferably the acrylic acid derivative is sodium acrylate.It is preferred that after step (iii) the stream P is subjected to one or more separation steps.240823W001- 15 - In the case where after step (iii) the stream P is subjected to one or more separation steps, and wherein R is Li, Na, K or Cs, it is preferred that the one or more separation steps comprise an extraction, wherein the extraction is more preferably performed using a polar solvent.In the case where the extraction is performed using a polar solvent, it is preferred that the polar solvent is selected from the group consisting of N,N-dimethylformamide, acetone, acetonitrile, methanol, ethanol, ethyl acetate, N-Methyl-2-pyrrolidon, and mixtures of two or more thereof, wherein more preferably the polar solvent is N,N-dimethylformamide.In the case where after step (iii) the stream P is subjected to one or more separation steps, and wherein R is C1-C4-alkyl, it is preferred that the one or more separation steps comprise a distillation.In the case where the one or more separation steps comprise a distillation, it is preferred that the one or more separation steps further comprise an extraction.It is preferred that a part of the stream SE is employed in the reaction of ethylene and oxygen to produce ethylene oxide.It is preferred that the reaction of ethylene and oxygen to produce ethylene oxide is performed in the presence of a catalyst CEO.In the case where the reaction of ethylene and oxygen to produce ethylene oxide is performed in the presence of a catalyst CEO , it is preferred that the catalyst CEO comprises one or more metals, more preferably one or more transition metals, and a support material.In the case where the catalyst CEO comprises one or more metals, it is preferred that the one or more metals, more preferably one or more transition metals, of the catalyst CEO comprise Ag.It is preferred that ethylene oxide is produced in a production unit comprising a main reactor, an ethylene oxide scrubber, and ethylene oxide desorber, a stripping column, a distillation column, a carbon dioxide scrubber, and a carbon dioxide de-scrubber.In the case where the production unit comprises a main reactor, an ethylene oxide scrubber, and ethylene oxide desorber, a stripping column, a distillation column, a carbon dioxide scrubber, and a carbon dioxide de-scrubber, it is preferred that at least part of the CO2 of the stream Sc is obtained from the carbon dioxide de-scrubber.It is preferred that in the cracking reaction a hydrocarbon feedstock is cracked to obtain a product of a cracking reaction, wherein the product of a cracking reaction more preferably comprises, more preferably consists of, a cracked gas comprising olefins.240823W001- 16 -In the case where in the cracking reaction a hydrocarbon feedstock is cracked to a obtain product of a cracking reaction, it is preferred that the hydrocarbon feedstock is selected from the group consisting of C2-C4-alkanes, (bio-)naphtha, gas oil, hydrocracker residues, and or mixtures of two or more thereof.In the case where the product of a cracking reaction comprises a cracked gas comprising olefins, it is preferred that the cracked gas comprises ethylene, wherein more preferably at least part or all of the ethylene comprised in said cracked gas is employed for preparing the stream SE in (ii).It is preferred that in the cracking reaction ammonia is cracked to obtain a product of a cracking reaction, wherein said product of a cracking reaction more preferably comprises, more preferably consists of, a cracked gas comprising nitrogen and hydrogenFurther in the case where in the cracking reaction a hydrocarbon feedstock or ammonia is cracked to obtain a product of a cracking reaction, it is preferred that the cracking of the hydrocarbon feedstock or of ammonia is effected in one or more crackers, wherein at least one of the crackers is, at least partially, directly or indirectly heated by combusting the carbonaceous fuel, wherein the combustion of the carbonaceous fuel generates the flue gas stream comprising carbon dioxide.It is preferred that the carbonaceous fuel comprises, more preferably consists of, any form of combustible matter which comprises carbon-containing compounds.It is preferred that obtaining at least part of the CO2 comprised in stream Sc from the flue gas comprises subjecting the flue gas stream to a carbon capture process.In the case where obtaining at least part of the CO2 comprised in stream Sc from the flue gas comprises subjecting the flue gas stream to a carbon capture process, it is preferred that the carbon capture process comprises(1) an absorption step, in which the flue gas stream is contacted with an absorbent in an absorber unit, obtaining an absorbent laden with carbon dioxide and a flue gas stream from which carbon dioxide has been at least partly removed;(2) a regeneration step, in which at least a portion of the carbon dioxide of the absorbent laden with carbon dioxide is removed from said absorbent in a regeneration unit, obtaining an at least partly regenerated absorbent and the at least part or all of the stream Sc.(3) a recycling step, in which at least a portion of the regenerated absorbent is recycled as the absorbent to step (1).240823W001- 17 -Acrylic acid and / or an acrylic acid derivative obtainable and / or obtained according to the process of the present invention having a low carbon footprint.Use of the process of process of the present invention to co-produce acrylic acid and / or acrylic acid derivatives parallel to the production of ethylene oxide and / or olefins.Within the meaning of the present invention, the term “at least part or all” relative to a stream of the inventive process preferably relates to the relative quantity of the total respective stream employed in the respective step, wherein the relative quantity is in the range of from >0 to 100 %, wherein more preferably in the case where the relative quantity is lower than 100 %, the respective stream is separated into two or more separate streams identical in their composition, wherein more preferably only one of said two or more separate streams is employed in the respective step of the inventive process. Within the meaning of the present invention, said term does not refer to the degree of the turnover of the respective stream in the respective step.The present invention further relates to a process as described above, preferably the process comprising (i) to (iii) as described above, wherein said process (further) comprises the step of converting the product stream P obtainable or obtained by the process described herein, or a chemical material obtainable or obtained by the process described herein, to obtain a product Q. Said product Q is preferably selected frombuilding block or monomer; orpolymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orcleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; oragrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; oractive pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; oraqueous 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; orcosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or240823W001- 18 - polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.Further regarding said product Q, it is preferred thatthe content of the product stream P obtainable or obtained by the process described herein in the product Q is 1 weight-% or more, more preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / orthe content of the product stream P obtainable or obtained by the process described herein in the product Q is 100 weight-% or less, more 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; andwherein the content is preferably 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 referred to in the preceding paragraph 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 referred to in the preceding paragraph.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 / orassembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / orforming, preferably foaming, extruding and / or molding; and / orfinishing, preferably coating and / or smoothing.In addition, the one or more step(s) are described in detail in Reference RF1; paragraphs

[1000] to

[8005] ,240823W001- 19 - The term “building block”, as used in the context of the product Q herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0°C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and / or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, 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 RF1.240823W001- 20 - The term “polymer product A”, as used in the context of the product Q herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is defined in more detail in paragraphs

[2009] and

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

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

[3035] to

[3044] of Reference RF1. The term “industrial use surfactant”, as used in the context of the product Q herein, comprises non-ionic, anionic and amphoteric industrial use 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 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] ,240823W001- 21 -The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer” and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof” may 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, propionic240823W001- 22 -acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1,2-propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinylimidazole / polyvinylpyrrolidone-co-polymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

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

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

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

[6002] entitled “Polyurethane dispersions” of240823W001- 23 - Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

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

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

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

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

[6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section

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

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

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

[6006] entitled “Binders for paper coating”section

[6007] entitled “Binders for fiber bonding”section

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

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

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

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

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

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

[6009] entitled “UV-crosslinkable poly(meth)acrylates for use in UV-curable solvent-free hot melt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1.240823W001- 24 - Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

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

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

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

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

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

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

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

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

[6020] of Reference RF1. The term “inorganic binder composition” comprising the polymeric dispersants), as used 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 the240823W001- 25 -context of the product Q herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

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

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

[7006] of Reference RF1. The term “further cosmetic ingredient”, as used in the context of the product Q herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Perstonal 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.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 3", 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 and 3". 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 co-producing acrylic acid and / or acrylic acid derivatives, preferably parallel to the production of ethylene oxide and / or a product of a cracking reaction, comprising (i) preparing a stream Sc comprising carbon dioxide;(ii) preparing a stream SE comprising ethylene;240823W001- 26 - (iii) reacting at least part or all of the stream Sc and at least part or all, preferably all, of the stream SE in the presence of a catalyst CA, obtaining a product stream P comprising acrylic acid, an acrylic acid derivative, or acrylic acid and an acrylic acid derivative;wherein at least part or all of the CO2 comprised in the stream Sc is obtained as a byproduct from a reaction of ethylene and oxygen to produce ethylene oxide, and / or wherein at least part or all of the CO2 comprised in the stream Sc is obtained from a flue gas stream from combustion of a carbonaceous fuel to produce heat for a cracking reaction.2. The process of embodiment 1 , wherein the process is a continuous process.3. The process of embodiment 1 or 2, wherein (ii) comprises(ii.A) converting a part of the stream Sc comprising CO2 by hydrogenation or by electrochemical reduction of CO2 contained in said part of the Stream Sc, obtaining a stream SPI comprising ethanol, or ethylene and ethanol;(ii.B) converting at least part or all, preferably all, of the ethanol comprised in the stream SPI to ethylene in the presence of a dehydration catalyst CD, obtaining a stream SP2 comprising ethylene.4. The process of embodiment 3, wherein the hydrogenation in (ii.A) comprises reacting the stream Sc in the presence of a hydrogenation catalyst CH, H2, and optionally a solvent. 5. The process of embodiment 4, wherein the catalyst CH comprises a metal selected from the group consisting of Al, Ti, Fe, Co, Ni, Cu, Mo, Ru, Rh, Pd, Ag, Ir Pt, Au, La, Ce, Ga, Zr and mixtures of two or more thereof.6. The process of any one embodiments 3 to 5, wherein the hydrogenation in (ii.A) is conducted at a temperature in the range of from 50 to 1000 °C, preferably in the range of from 200 to 900 °C, more preferably in the range of from 350 to 850 °C.7. The process of embodiment 3, wherein the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of a cathode and an anode,wherein the cathode comprises C, Cu, Ag, Zn, Sn, In, Ga, Au or mixtures of two or more thereof,wherein the anode comprises C, Ir, Ru, Pt, Ni, Co, La, Sr, Fe Fe, , or mixtures of two or more thereof.8. The process of embodiment 7, wherein the cathode comprises Cu, wherein the cathode is selected from the group consisting of elemental Cu, nanostructured Cu, Cu nanoparticles, oxidized Cu, Cu foams, doped Cu, Cu alloys, Cu-based bimetallic catalysts, Cu-based240823W001- 27 - core-shell catalysts, Cu- and carbon-based hybrid materials, Cu phosphides, Cu-based metal-organic frameworks, and mixtures of two or more thereof.9. The process of embodiment 8, wherein the Cu alloys are selected from the group consisting of Cu-Ag, Cu-Zn, Cu-Sn, and mixtures of two or more thereof.10. The process of embodiment 8 or 9, wherein the Cu-based bimetallic catalysts are selected from the group consisting of Cu-ln, Cu-Ga, Cu-Au, and mixtures of two or more thereof.11. The process of any one of embodiments 8 to 10, wherein the Cu- and carbon-based hybrid materials are selected from the group consisting of Cu-graphene, Cu-graphite, Cu- carbon nanotubes, and mixtures of two or more thereof.12. The process of any one of embodiments 7 to 11, wherein the anode is selected from the group consisting of Ir-oxide, Ru-oxide, Ni foam, Ni-oxide, Ni-hydroxide, Ni-Fe alloy, Ni-Fe- oxide, Co-oxide, Co-Fe alloy, perovskite oxides, Pt, carbon-based materials, and mixtures of two or more thereof.13. The process of embodiment 12, wherein the carbon-based materials are selected from the group consisting of graphene, carbon nanotubes, hybrid composite supports, and mixtures of two or more thereof.14. The process of any one of embodiments 7 to 13, wherein the cathode and / or the anode comprise a dopant, wherein the dopant is preferably selected from the group consisting of Ca, V, Ti, Fe, Co, Ni, Cu, Nd, Hf, Eu, and mixtures of two or more thereof.15. The process of any one of embodiments 3 or 7 to 14, wherein the electrochemical reduction in (ii.A) comprises reacting the stream Sc in the presence of an electro-catalyst CE.16. The process of embodiment 15, wherein the catalyst CE is selected from the group consisting of metals, metal oxides, metal complexes, metal organic frameworks, metal-free electro-catalysts, and mixtures of two or more thereof.17. The process of embodiment 15 or 16, wherein the catalyst CE is coated on the cathode or the anode.18. The process of any one of embodiments 3 to 17, wherein the process after (ii.A) and prior to (ii.B) comprises(11.5.1) independently from each other separating ethylene and ethanol from the stream SPI, obtaining at least part or all of the stream SE, a stream comprising ethanol, and a stream SPI depleted of ethylene and ethanol;(11.5.2) feeding the stream comprising ethanol obtained in (ii.S.1) into step (ii.B).240823W001- 28 -19. The process of any one of embodiments 3 to 18, wherein the catalyst CD in (ii.B) comprises an oxidic material, wherein preferably the oxidic material is selected from the group consisting of a metal oxide, a molecular sieve, a heteropolyacid, and mixtures of two or more thereof.20. The process of any one of embodiment 3 to 19, wherein the process after (ii.B) further comprisesa step of separating ethylene from the stream SP2 to obtain at least part or all of the stream SE.21. The process of embodiment 1 or 2, wherein (ii) comprises(ii.A) converting a part of the stream Sc comprising CO2 by hydrogenation or by electrochemical reduction of CO2 contained in said part of the Stream Sc, obtaining a stream SPI comprising ethylene.22. The process of embodiment 21 , wherein the process after (ii.A) further comprisesa step of separating ethylene from the stream SPI to obtain at least part or all of the stream SE.23. The process of embodiment 1 or 2, wherein (ii) comprises(ii.a) preparing a stream SOH comprising an alcohol;(ii.b) converting at least part or all, preferably all, of the stream SOH, obtaining a stream So comprising ethylene, propylene, or ethylene and propylene(ii.c) separating ethylene from the stream So, obtaining at least part or all of the stream SE and a stream So depleted of ethylene.24. The process of embodiment 3 wherein the alcohol of the stream SOH is selected from the group consisting of methanol, ethanol, 1-propanol, 2-propanol ,1-butanol, 2-butanol, 1- pentanol, 1-hexanol, 1-heptanol, and mixtures of two or more thereof, preferably from the group consisting of methanol and ethanol, wherein more preferably the alcohol of the stream SOH comprises, preferably consists of, ethanol.25. The process of embodiment 23 or 24, wherein (ii.a) comprises(ii.a.1) preparing a stream SH comprising H2;(ii.a.2) reacting at least part of the stream Sc with at least part or all of the stream SH in the presence of a gas shift catalyst CGS, obtaining a stream Ss comprising H2 and CO;240823W001- 29 - (ii.a.3) converting at least part or all, preferably all, of the stream Ss in the presence of an alcohol formation catalyst COH, obtaining the stream SOH.26. The process of embodiment 25, wherein the reaction in step (ii.a.2) is a reverse water gas shift reaction, wherein the following reaction occurs:CO2+ H2CO + H2O27. The process of embodiment 25 or 26, wherein the catalyst CGS in step (ii.a.2) comprises a metal selected from the group consisting of Ni, Co, Fe Cu, Zn, Mn, Pd, Pt, Rh, Zr, In, Ga, La, Ce, and mixtures of two or more thereof.28. The process of any one of embodiments 25 to 26, wherein converting the stream Ss in step (ii.a.3) comprises reacting said stream with a part of the stream SH in the presence of the catalyst COH.29. The process of any one of embodiments 25 to 28, wherein the catalyst COH in step (ii.a.3) comprises a metal selected from the group consisting of Fe, Co, Cu, Zn, Mo, Ru, Rh, Pd, Pt, Au, and mixtures of two or more thereof.30. The process of any one of embodiments 25 to 29, wherein the alcohol comprised in the stream SOH obtained in step (ii.a.3) is ethanol and one or more of 1-propanol, 2-propanol, 1-butanol, 2-butanol, and 2-methyl-1 -propanol, preferably one or more of 1-butanol, 2-bu- tanol, and 2-methyl-1 -propanol.31. The process of any one of embodiments 25 to 30, wherein the catalyst CGS and the catalyst COH are the same catalyst.32. The process of embodiment 23 or 24, wherein (ii.a) comprises a fermentation of glucose, obtaining the stream SOH comprising, preferably consisting of, ethanol, wherein at least part of the CO2 comprised in the stream Sc is further obtained as a by-product.33. The process of any one of embodiments 23 to 32, wherein SOH comprises, preferably consists of, ethanol, wherein (ii.b) comprises converting at least part or all of the stream SOH in the presence of a dehydration catalyst CD, obtaining the stream So comprising ethylene34. The process of embodiment 33, wherein the catalyst CD comprises an oxidic material, wherein preferably the oxidic material is selected from the group consisting of a metal oxide, a molecular sieve, a heteropolyacid, and mixtures of two or more thereof.240823W001- 30 - 35. The process of embodiment 33 or 34, wherein the step (ii.b) is conducted at a temperature in the range of from 100 to 800 °C, preferably in the range of from 200 to 600 °C, more preferably in the range of from 300 to 500 °C.36. The process of any one of embodiments 33 to 35, wherein the step (ii.b) is conducted at a pressure in the range of from 0.1 to 20 bar(abs), preferably in the range of from 0.5 to 10 bar(abs), more preferably in the range of from 1 to 2 bar(abs).37. The process of any one of embodiments 23 to 36, wherein SOH comprises, preferably consists of, ethanol and wherein only part of the stream SOH is converted in step (ii.b), wherein the process further comprises(iv) converting at least part or all, preferably all, of the stream SOH that is not employed in step (ii.b) in the presence of one or more catalysts, obtaining a stream SP comprising propylene.38. The process of embodiment 37, wherein step (iv) comprises(iv.1 ) converting the stream SOH in the presence of the dehydration catalyst CD, obtaining a stream comprising ethylene;(iv.2) converting the stream comprising ethylene in the presence of one or more catalysts, obtaining the stream SP comprising propylene.39. The process of embodiment 38, wherein converting in step (iv.2) is performed in the presence of a oligomerization catalyst CEP.40. The process of embodiment 39, wherein the catalyst CD and the catalyst CEP are the same catalyst.41. The process of embodiment 40, wherein step (iv.2) comprises(iv.2.1) converting the stream comprising ethylene in the presence of a dimerization catalyst CDM, obtaining a stream comprising 2-butene;(iv.2.11) converting the stream comprising 2-butene in the presence of a metathesis catalyst CM, obtaining the stream SP comprising propylene.42. The process of embodiment 41 , wherein the catalyst CDM and the catalyst CM are the same catalyst.43. The process of embodiment 41 or 42, wherein the catalysts CD, CDM and CM are the same catalyst.44. The process of embodiment 38, wherein step (iv.2) comprises(iv.2.1’) converting the stream comprising ethylene in the presence of a trimerization240823W001- 31 - catalyst CTM, obtaining a stream comprising 1 -hexene;(iv.2. II’) converting the stream comprising 1-hexene in the presence of a p-fission catalyst CBF, obtaining the stream SP comprising propylene.45. The process of embodiment 44, wherein the catalyst CTM and the catalyst CBF are the same catalyst.46. The process of embodiment 44 or 45, wherein the catalysts CD, CTM and CBF are the same catalyst.47. The process of any one of embodiments 38 to 46, wherein the catalysts CD, CEP, CDM, CM, CTM and CBF comprise acidic active sites.48. The process of embodiment 47, wherein the catalysts CD, CEP, COM, CM, and CBF comprise a zeolitic material having a framework structure type selected from the group consisting of AEI, BEA, ERI, EUO, FAU, FER, GIS, HEU, LTA, LTL, MFI, MOR, MTW, MWW, RHO, and mixtures of two or more thereof, preferably AEI, BEA, CHA or MFI, more preferably MFI.49. The process of embodiment 48, wherein the zeolitic material further comprises a metal selected from the group consisting of Mg, Ca, Ba, Sr, Fe, Cr, Ce, Co, Cu, Ni, Zr, Mo, Ag, Au, W, La, Pd, Pt, Ru, Rh, Re, Ir, and mixtures of two or more thereof.50. The process of embodiment 37, wherein step (iv) comprises(iv.T) converting a part of the stream SOH in the presence of a dehydrogenate catalyst CEA, obtaining a stream comprising acetaldehyde;(iv.2’) converting the stream comprising acetaldehyde in the presence of a ketonization catalyst CAA, obtaining a stream comprising acetone;(iv.3’) converting the stream comprising acetone in the presence of a hydrogenationdehydration catalyst CAP, obtaining the stream SP comprising propylene.51. The process of embodiment 50, wherein the catalysts CEA, CAA and CAP are the same catalyst.52. The process of embodiment 50 or 51 , wherein the catalysts CEA, CAA and CAP comprise basic active sites.53. The process of embodiment 52, wherein the catalysts CEA, CAA and CAP comprise a metal oxide.240823W001- 32 - 54. The process of embodiment 53, wherein the metal in the metal oxide is selected from the group consisting of Y, Ce, Zr, In, and mixtures of two or more thereof.55. The process of embodiment 53 or 54, wherein the catalysts CEA, CAA and CAP further comprise a zeolitic material.56. The process of embodiments 55, wherein the zeolitic material has framework structure type selected from the group consisting of AEI, BEA, ERI, EUO, FAU, FER, GIS, HEU, LTA, LTL, MFI, MOR, MTW, MWW, RHO, and mixtures of two or more thereof, preferably AEI, BEA, CHA or MFI, more preferably BEA.57. The process of embodiment 23 or 24, wherein (ii.a) comprises converting a part of the stream Sc by hydrogenation or by electrochemical reduction, obtaining the stream SOH comprising methanol.58. The process of any one of embodiments 23 to 57, wherein SOH comprises, preferably consists of, methanol, wherein (ii.b) comprises(ii.b.l) converting at least part or all, preferably all, of the stream SOH in in the presence of a methanol-to-olefin catalyst Cmto, obtaining the stream So comprising ethylene and propylene;(ii.b. II) separating ethylene from the stream So, obtaining at least part or all of the stream SE and a stream So depleted of ethylene.59. The process of embodiment 58, further comprising(ii.b. Ill) separating propylene from the stream So depleted of ethylene, obtaining the stream SP.60. The process of embodiment 58 or 59, wherein the catalyst Cmto comprises a zeolitic material having a framework structure type selected from the group consisting of AEI, BEA, ERI, EUO, FAU, FER, GIS, HEU, LTA, LTL, MFI, MOR, MTW, MWW, RHO, or mixtures of two or more thereof, preferably AEI, BEA, CHA or MFI, more preferably CHA.61. The process of embodiment 60, wherein the zeolitic material comprises H-beta, ZSM-22, ZSM-5 and / or SAPO-34.62. The process of any one of embodiments 58 to 61 , wherein the step (ii.b.l) is conducted at a temperature in the range of from 100 to 1000 °C, preferably in the range of from 200 to 800 °C, more preferably in the range of from 350 to 600 °C.240823W001- 33 - 63. The process of any one of embodiments 58 to 62, wherein the step (ii.b.l) is conducted at a pressure in the range of from 0.1 to 20 bar(abs), preferably in the range of from 0.5 to 10 bar(abs), more preferably in the range of from 1 to 3 bar(abs)64. The process of any one of embodiments 23 to 63, wherein propylene is comprised in the stream So or the stream SP is obtained, wherein the process further comprises(v) converting at least part or all of the propylene comprised in the stream So orthe stream SP in the presence of oxygen and an oxidation catalyst Co, obtaining a product stream PA comprising acrylic acid.65. The process of any one of embodiments 23 to 64, wherein propylene is comprised in the stream So or the stream SP is obtained, wherein the process further comprises(v’) converting at least part or all of the propylene comprised in the stream So orthe stream SP in the presence of a hydroformylation catalyst CB, obtaining a stream SB comprising butanol;(vi’) converting at least part or all of the stream SB, obtaining a product stream PB comprising butyl acrylate.66. The process of embodiment 65, wherein converting in the step (v’) comprises the steps of a hydroformylation and a hydrogenation.67. The process of embodiment 66, wherein the catalyst CB is present in the hydroformylation step.68. The process of embodiment 65 to 67, wherein the step (vi’) comprises reacting at least part or all of the stream SB with acrylic acid or an acrylic acid derivative.69. The process of any one of embodiments 1 to 68, wherein the catalyst CA in step (iii) comprises a metal complex comprising a metal MA and a ligand LA.70. The process of embodiment 69, wherein the metal MA is selected from the group consisting of Fe, Ni, Co, Mo, Pd, Ru, Rh, Ir, Pt, W, Ag, Au, and mixtures of two or more thereof.71. The process of embodiment 69 or 70, wherein the ligand LA is selected from the group consisting of amine ligands, phosphine ligands, olefin ligands, and mixtures of two or more thereof.72. The process of any one of embodiments 1 to 71, wherein reacting in step (iii) is carried out in the the presence of a base.240823W001- 34 - 73. The process of any one of embodiments 1 to 72, wherein reacting in step (iii) is carried out in the presence of a solvent.74. The process of any one of embodiments 1 to 73, wherein reacting in step (iii) is carried out in the presence of a reductant and / or an alkylation agent.75. The process of any one of embodiments 1 to 74, wherein the reacting in step (iii) is conducted at a temperature in the range of from 25 to 1200 °C, preferably in the range of from 100 to 800 °C, more preferably in the range of from 200 to 500 °C.76. The process of any one of embodiments 1 to 75, wherein the reacting in step (iii) is conducted at a pressure in the range of from 0.1 to 400 bar(abs), preferably in the range of from 10 to 200 bar(abs), more preferably in the range from 50 to 150 bar(abs).77. The process of any one of embodiments 1 to 76, wherein the acrylic acid derivative comprise the general formula (A)wherein X is N, O, or S;wherein R is H, Li, Na, K, Cs or C1-C4-alkyl.78. The process of embodiment 77, wherein the acrylic acid derivative is selected from the group consisting of lithium acrylate, sodium acrylate, methyl acrylate, ethyl acrylate, and mixtures of two or more thereof, wherein preferably the acrylic acid derivative is sodium acrylate.79. The process of any one of embodiments 1 to 78, wherein after step (iii) the stream P is subjected to one or more separation steps.80. The process of embodiment 79, wherein R is Li, Na, K or Cs, wherein the one or more separation steps comprise an extraction, wherein the extraction is preferably performed using a polar solvent.81. The process of embodiment 80, wherein the polar solvent is selected from the group consisting of N,N-dimethylformamide, acetone, acetonitrile, methanol, ethanol, ethyl acetate, N-Methyl-2-pyrrolidon, and mixtures of two or more thereof, wherein preferably the polar solvent is N,N-dimethylformamide.82. The process of embodiment 81, wherein R is C1-C4-alkyl, wherein the one or more separation steps comprise a distillation.240823W001- 35 -83. The process of embodiment 82, wherein the one or more separation steps further comprise an extraction.84. The process of any one of embodiments 1 to 83, wherein a part of the stream SE is employed in the reaction of ethylene and oxygen to produce ethylene oxide.85. The process of any one of embodiments 1 to 84, wherein the reaction of ethylene and oxygen to produce ethylene oxide is performed in the presence of a catalyst CEO.86. The process of embodiment 85, wherein the catalyst CEO comprises one or more metals, preferably one or more transition metals, and a support material.87. The process of embodiment 86, wherein the one or more metals, preferably one or more transition metals, of the catalyst CEO comprise Ag.88. The process of any one of embodiments 1 to 87, wherein ethylene oxide is produced in a production unit comprising a main reactor, an ethylene oxide scrubber, and ethylene oxide desorber, a stripping column, a distillation column, a carbon dioxide scrubber, and a carbon dioxide de-scrubber.89. The process of embodiment 88, wherein the at least part of the CO2 of the stream Sc is obtained from the carbon dioxide de-scrubber.90. The process of any one of embodiments 1 to 89, wherein in the cracking reaction a hydrocarbon feedstock is cracked to obtain a product of a cracking reaction, wherein the product of a cracking reaction preferably comprises, more preferably consists of, a cracked gas comprising olefins.91. The process of embodiment 90, wherein the hydrocarbon feedstock is selected from the group consisting of C2-C4-alkanes, (bio-)naphtha, gas oil, hydrocracker residues, and or mixtures of two or more thereof.92. The process of embodiment 90 or 91 , wherein the cracked gas comprises ethylene, wherein preferably at least part or all of the ethylene comprised in said cracked gas is employed for preparing the stream SE in (ii).93. The process of any one of embodiments 1 to 89, wherein in the cracking reaction ammonia is cracked to obtain a product of a cracking reaction, wherein said product of a cracking reaction preferably comprises, more preferably consists of, a cracked gas comprising nitrogen and hydrogen.240823W001- 36 -94. The process of any one of embodiments 90 to 93, wherein the cracking of the hydrocarbon feedstock or of ammonia is effected in one or more crackers, wherein at least one of the crackers is, at least partially, directly or indirectly heated by combusting the carbonaceous fuel, wherein the combustion of the carbonaceous fuel generates the flue gas stream comprising carbon dioxide.95. The process of any one of embodiments 1 to 94, wherein the carbonaceous fuel comprises, preferably consists of, any form of combustible matter which comprises carbon- containing compounds.96. The process of any one of embodiments 1 to 95, wherein obtaining at least part of the CO2 comprised in stream Sc from the flue gas comprises subjecting the flue gas stream to a carbon capture process.97. The process of embodiment 96, wherein the carbon capture process comprises(1) an absorption step, in which the flue gas stream is contacted with an absorbent in an absorber unit, obtaining an absorbent laden with carbon dioxide and a flue gas stream from which carbon dioxide has been at least partly removed;(2) a regeneration step, in which at least a portion of the carbon dioxide of the absorbent laden with carbon dioxide is removed from said absorbent in a regeneration unit, obtaining an at least partly regenerated absorbent and the at least part or all of the stream Sc.(3) a recycling step, in which at least a portion of the regenerated absorbent is recycled as the absorbent to step (1).98. Acrylic acid and / or an acrylic acid derivative obtainable and / or obtained according to the process of any one of embodiments 1 to 97 having a low carbon footprint.99. Use of the process of any one of embodiments 1 to 97 to co-produce acrylic acid and / or acrylic acid derivatives parallel to the production of ethylene oxide and / or olefins.100. A process, preferably according to any of embodiments 1 to 97, comprising the step of converting the product stream P obtainable or obtained by the process of any of embodiments 1 to 97 to obtain a product Q.101. The process of embodiment 100, wherein the product Q is selected from:building block or monomer; orpolymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orcleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition or formulation thereof; or240823W001-37 - agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; oractive pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; oraqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth) acrylate 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 composi-tions, unsaturated polyester polyol or 100% curable composition; orcosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; orpolymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate102. The process of embodiment 100 or 101,wherein the content of the product stream P obtainable or obtained by the process of any one of embodiments 1 to 97 in the product Q is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / orwherein the content of the product stream P obtainable or obtained by the process of any one of embodiments 1 to 97 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; and preferably wherein the 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.CITED LITERATURE- X. Wang, H. Wang, and Y. Sun, “Synthesis of Acrylic Acid Derivatives from CO2 and Ethylene,” Chem, vol. 3, no. 2, pp. 211-228, Aug. 2017M. Zhang and Y. Yu, “Dehydration of Ethanol to Ethylene,” Ind. Eng. Chem. Res., vol.52, no. 28, pp. 9505-9514, Jul. 2013240823W001- 38 - - A. M. Bahmanpour, M. Signorile, and O. Krdcher, “Recent progress in syngas production via catalytic CO2 hydrogenation reaction,” Applied Catalysis B: Environmental, vol. 295, p. 120319, Oct. 2021S. S. Ali, S. S. Ali, and N. Tabassum, “A review on CO2 hydrogenation to ethanol: Reaction mechanism and experimental studies,” Journal of Environmental Chemical Engineering, vol. 10, no. 1, p. 106962, Feb. 2022L. Petrescu, M. Fermeglia, and C.-C. Cormos, “Life Cycle Analysis applied to acrylic acid production process with different fuels for steam generation,” Journal of Cleaner Production, vol. 133, pp. 294-303, Oct. 2016P. Tian, Y. Wei, M. Ye, and Z. Liu, “Methanol to Olefins (MTO): From Fundamentals to Commercialization,” ACS Catal., vol. 5, no. 3, pp. 1922-1938, Mar. 2015- X. Jiang et al., “Recent Advances in Carbon Dioxide Hydrogenation to Methanol via Heterogeneous Catalysis”, Chem. Rev., vol. 120, no. 15, pp. 7984-8034, Feb. 2020 S. Nitopi et al., “Progress and Perspectives of Electrochemical CO2 Reduction on Copper in Aqueous Electrolyte,” Chem. Rev., vol. 119, no. 12, pp. 7610-7672, Jun.2019K. Wiranarongkorn, K. Eamsiri, Y.-S. Chen, A. Arpornwichanop, “A comprehensive review of electrochemical reduction of CO2 to methanol: Technical and design aspects” J. CO2 Util., vol. 71, 102477, May 2023- X. Cui, S. K. Kaer, “A comparative study on three reactor types for methanol synthesis from syngas and CO2”, Chem. Eng. J., vol. 393, article 124632, Aug. 2020- Y. Mao et al., “Progress in the thermo-catalytic hydrogenation of CO2 to ethanol”, J.Fuel Chem. Technol., vol 51, no. 10, pp. 1514-1528, Oct. 2023- A. I. Latsiou et al., “CO2 hydrogenation for the production of higher alcohols: Trends in catalyst developments, challenges and opportunities”, Catalysis today, vol. 420, article 114179, Aug. 2023T. Lu et al., “Electrocatalytic CO2 Reduction to Ethylene: From Advanced Catalyst Design to Industrial Applications”, Adv. Mater., vol. 35, article 202310433, Nov. 2023 I. Jang et al., “Electrocatalysis in Solid Oxide Fuel Cells and Electrolyzers”, Chem. Rev., vol. 124, pp. 8233-8306, June 2024R. Chauhan et al., “Advancements in Environmentally Sustainable Technologies for Ethylene Production”, Energy Fuels, vol. 37, pp. 12589-12622, Aug. 2023- WO 2019 / 053540 A 1- WO 2024 / 132696 A 1- US 2011 / 112314 A1- WO 03 / 055869 A1

Claims

240823W001- 39 - Claims1. A process for co-producing acrylic acid and / or acrylic acid derivatives parallel to the production of ethylene oxide and / or a product of a cracking reaction, comprising(i) preparing a stream Sc comprising carbon dioxide;(ii) preparing a stream SE comprising ethylene;(iii) reacting at least part or all of the stream Sc and at least part or all, preferably all, of the stream SE in the presence of a catalyst CA, obtaining a product stream P comprising acrylic acid, an acrylic acid derivative, or acrylic acid and an acrylic acid derivative;wherein at least part or all of the CO2 comprised in the stream Sc is obtained as a byproduct from a reaction of ethylene and oxygen to produce ethylene oxide, and / or wherein at least part or all of the CO2 comprised in the stream Sc is obtained from a flue gas stream from combustion of a carbonaceous fuel to produce heat for a cracking reaction.

2. The process of claim 1, wherein in the cracking reaction a hydrocarbon feedstock is cracked to obtain a product of a cracking reaction, wherein the product of a cracking reaction comprises, preferably consists of, a cracked gas comprising ethylene, wherein at least part or all of the ethylene comprised in said cracked gas is employed for preparing the stream SE in (ii).

3. The process of claim 1 or 2, wherein (ii) comprises(ii.A) converting a part of the stream Sc comprising CO2 by hydrogenation or by electrochemical reduction of CO2 contained in said part of the Stream Sc, obtaining a stream SPI comprising ethanol, or ethylene and ethanol;(ii.B) converting at least part or all, preferably all, of the ethanol comprised in the stream SPI to ethylene in the presence of a dehydration catalyst CD, obtaining a stream SP2 comprising ethylene.

4. The process of claim 1 or 2, wherein (ii) comprises(ii.A) converting a part of the stream Sc comprising CO2 by hydrogenation or by electrochemical reduction of CO2 contained in said part of the Stream Sc, obtaining a stream SPI comprising ethylene.

5. The process of claim 1 or 2, wherein (ii) comprises(ii.a) preparing a stream SOH comprising an alcohol;(ii.b) converting at least part or all, preferably all, of the stream SOH, obtaining a stream So240823W001-40 - comprising ethylene, propylene, or ethylene and propylene(ii.c) separating ethylene from the stream So, obtaining at least part or all of the stream SE and a stream So depleted of ethylene.

6. The process of claim 5, wherein (ii.a) comprises(ii.a.1) preparing a stream SH comprising H2;(ii.a.2) reacting at least part of the stream Sc with at least part or all of the stream SH in the presence of a gas shift catalyst CGS, obtaining a stream Ss comprising H2 and CO;(ii.a.3) converting at least part or all, preferably all, of the stream Ss in the presence of an alcohol formation catalyst COH, obtaining the stream SOH.

7. The process of claim 5, wherein (ii.a) comprises a fermentation of glucose, obtaining the stream SOH comprising, preferably consisting of, ethanol, wherein at least part of the CO2 comprised in the stream Sc is further obtained as a by-product.

8. The process of any one of claims 5 to 7, wherein SOH comprises, preferably consists of, ethanol, wherein (ii.b) comprises converting at least part or all of the stream SOH in the presence of a dehydration catalyst CD, obtaining the stream So comprising ethylene9. The process of any one of claims 5 to 8, wherein SOH comprises, preferably consists of, ethanol and wherein only part of the stream SOH is converted in step (ii.b), wherein the process further comprises(iv) converting at least part or all, preferably all, of the stream SOH that is not employed in step (ii.b) in the presence of one or more catalysts, obtaining a stream SP comprising propylene.

10. The process of any one of claims 5 to 9, wherein SOH comprises, preferably consists of, methanol, wherein (ii.b) comprises(ii.b. I) converting at least part or all, preferably all, of the stream SOH in in the presence of a methanol-to-olefin catalyst Cmto, obtaining the stream So comprising ethylene and propylene;(ii.b. II) separating ethylene from the stream So, obtaining at least part or all of the stream SE and a stream So depleted of ethylene.

11. The process of any one of claims 5 to 10, wherein propylene is comprised in the stream So or the stream SP is obtained, wherein the process further comprises(v) converting at least part or all of the propylene comprised in the stream So or240823W001- 41 - the stream SP in the presence of oxygen and an oxidation catalyst Co, obtaining a product stream PA comprising acrylic acid.

12. The process of any one of claims 5 to 11 , wherein propylene is comprised in the stream So or the stream SP is obtained, wherein the process further comprises(v’) converting at least part or all of the propylene comprised in the stream So orthe stream SP in the presence of a hydroformylation catalyst CB, obtaining a stream SB comprising butanol;(vi’) converting at least part or all of the stream SB, obtaining a product stream PB comprising butyl acrylate.

13. The process of any one of claims 1 to 12, wherein the acrylic acid derivative comprises the general formula (A)wherein X is N, O, or S;wherein R is H, Li, Na, K, Cs or C1-C4-alkyl.

14. Use of the process of any one of claims 1 to 13 to co-produce acrylic acid and / or acrylic acid derivatives parallel to the production of ethylene oxide and / or a product of a cracking reaction.

15. A process according to any one of claims 1 to 13, comprising the step of converting the product stream P obtainable or obtained by the process of any one of claims 1 to 13 to obtain a product Q.

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