Process for preparing syngas using a plasma feed

Abstract

The present invention relates to a process for preparing syngas, the process comprising (i) preparing a first feed stream comprising one or more organic compounds; (ii) preparing a second feed stream comprising CO2 and optionally comprising O2; (iii) optionally preparing a third feed stream comprising steam; (iv) heating the second feed stream, or optionally combining and heating the first and second feed streams, or optionally combining and heating the second and third feed streams, or optionally combining and heating the first, second, and third feed streams, wherein the feed stream or the optionally combined feed streams are heated to a temperature in the range of from 1,000 to 20,000 °C; (v) combining the heated second feed stream obtained in (iv) with the first feed stream and optionally with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined first and second feed streams obtained in (iv) with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined second and third feed streams obtained in (iv) with the first feed stream, obtaining a reaction stream; (vi) feeding the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v) in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2 and H2O, wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

Description

[0001] Process for preparing syngas using a plasma feed

[0002] TECHNICAL FIELD

[0003] The present invention relates to a process for preparing syngas (also known as synthesis gas) via partial oxidation reaction of one or more organic compounds, wherein a plasma feed stream comprising one or more of CO2 and steam is prepared for introducing the necessary energy for converting one or more organic compounds to CO and hydrogen.

[0004] INTRODUCTION

[0005] Generally, syngas comprises H2and CO, wherein one or both of CO2and H2O can be comprised as well. Depending on the need, syngas can be prepared having a specific H2to CO molar ratio. Preparation of syngas is typically done by partial oxidation of organic compounds in the presence of one or more of O2and steam. CO2can be generated as side-product and it can be separated from a product stream. Separated CO2can also be recycled into the preparation process as a reactant. Usually, the energy needed for the conversion of the one or more organic compounds is provided by partial or complete oxidation reactions thereof resulting in a certain amount of CO2as side-product.

[0006] WO 2015 / 090575 A1 generally relates to a method and device for producing syngas.

[0007] WO 2022 / 200532 A1 relates to a method for producing a synthesis gas mixture containing hydrogen and carbon monoxide by means of non-catalytic partial oxidation of an organic feedstock in the presence of oxygen and carbon dioxide, in which method at least a reactant gas containing one or more organic feedstocks, a reactant gas containing oxygen, and a reactant gas containing carbon dioxide are fed into a partial oxidation reactor and are reacted at a temperature in the range of 1200 to 1550 °C to obtain a product gas mixture containing hydrogen, carbon monoxide and carbon dioxide, with at least a portion of the carbon dioxide being separated off from the product gas mixture and fed back into the partial oxidation reactor. The method is characterized in that the carbon dioxide fed into the partial oxidation reactor contains additional, imported carbon dioxide, with a product gas mixture having a molar ratio of hydrogen to carbon monoxide in the range of 0.8:1 to 1.6:1 being obtained in the partial oxidation reactor.

[0008] US 10435295 B2 relates to a method of preparing liquid fuels from syngas, the method particularly comprising: providing a waste conversion reactor having a decomposition chamber wherein waste materials comprising organic and inorganic waste is pyrolyzed to produce a high temperature syngas from said organic material and slag from decomposition of said inorganic waste; said waste conversion reactor comprising a submerged arc furnace or plasma torch furnace which supplies heat to the decomposition chamber for pyrolysis and decomposition of said organic and inorganic waste materials; and introducing said syngas to a liquid fuel synthesis system comprising one or more synfuel conversion reactors wherein said syngas is converted into liquid fuel. In claim 7 it is disclosed that one or more effluent stream from said synfuel conversion reactor comprising water, carbon dioxide and tail gas can be introduced into said waste conversion reactor.

[0009] US 2014 / 0239232 A1 relates to a hydrocarbon pyrolysis unit comprising: a plurality of plasma torches that are located within the hydrocarbon pyrolysis unit in an arrangement that causes an operation of the plurality of plasma torches to create a pyrolysis zone that increases an efficiency of the hydrocarbon pyrolysis unit in breaking atomic bonds of hydrocarbon material that is located within the hydrocarbon pyrolysis unit during a plasma pyrolysis process. According to claim 7, the pyrolysis unit further comprises a carbon dioxide recycle loop that recycles carbon dioxide to the hydrocarbon pyrolysis unit from the synthetic gas preparation process of the hydrocarbon pyrolysis unit.

[0010] US 2016 / 0362355 A1 relates to preparation of an oil product of gasoline. The product contains hydrocarbon compounds ranged as a gasoline composition. The purification process of dimethyl ether (DME) used can reduce the feed rate for obtaining a smaller reactor with cost advantages. Carbon dioxide (CO2) can be separated to be recycled back to the gasifier to be reused or sequestrated. At the same time, CO2 can be reacted with hydrocarbons, water vapor, etc. through a high-temperature plasma torch to generate a synthesis gas (syngas) of carbon monoxide (CO) and hydrogen (H2) for regulating a hydrogen / carbon ratio of a biomass- or hydrocarbon- synthesized compound and helping subsequent chemical synthesis reactions. In the end, the final gasoline production has a high yield, a high octane number, low nitrogen and sulfur contamination and a high quality.

[0011] WO 2021 / 180482 A1 discloses a process for the production of synthesis gas by gasification, preferably by plasma gasification, of carbon-containing material using a gasification gas comprising at least 2 mol% carbon dioxide, and optionally at least one gas selected from steam, oxygen, hydrogen, methane and air, wherein external energy obtained from electric power is supplied in the gasification step and wherein exhaust gas of the process comprising carbon dioxide is at least partially recycled back into the gasification step. Furthermore, the invention proposes a process for production of synthesis gas downstream products, wherein the synthesis gas is produced by the process and used as an intermediate product in a downstream synthesis process.

[0012] US 2022 / 234889 A1 relates to a system for manufacturing a nanomaterial may include a first electrode; a second electrode spaced apart from the first electrode by a gap; and a chamber configured to enclose the first electrode, the second electrode, and a liquid. The system may also include a power supply configured to provide electrical energy to at least one of the first electrode and the second electrode; and a pump configured to cause the liquid to flow through the gap between the first electrode and the second electrode. KR 101882813 B1 relates to a reforming reactor for producing syngas from methane or from a source of methane containing CO2such as natural gas, biogas, landfill gas, and coal gas, wherein unreacted methane is recycled to the reforming reactor.

[0013] Thus, there was a need to provide a process for preparing syngas allowing reduction of CO2generated as side-product.

[0014] It was therefore an object to provide a process for preparing syngas achieving a reduction of produced CO2. In addition, it was an object to provide a process for preparing syngas particularly allowing processing of a liquid feedstock. Further, it was an object to provide a process for preparing syngas allowing recycling of CO2allowing a reduction of needed amounts of O2and steam.

[0015] Surprisingly, it has been found that syngas can be prepared by reacting a feed stream comprising one or more organic compounds with one or more plasma feed streams comprising CO2and / or steam. It has been found that the process of the present invention particularly allows introducing energy needed for the conversion of the one or more organic compounds differently, while particularly allowing a reduction of generated CO2as side-product, which can be recycled into the process as a reactant. Also, it was found that CO2stemming from other processes can be introduced as reactant. The process itself can be carried out in an even more efficient manner by injecting, optionally by spraying, the one or more organic compounds with the CO2. Thus, it has surprisingly been found that a process for preparing syngas can be provided achieving a comparatively reduced carbon footprint reported by CO2emissions. The CO to H2molar ratio of the prepared syngas can be adjusted by adding hydrogen, e.g. green or blue hydrogen. Additionally, it has been found that the process according to the present invention allows direct generation of syngas without further preliminary steps, e.g. pre-reforming. Thus, the process of the present invention is comparatively more efficient.

[0016] Further, it is possible to flexibly integrate electrical power that is available, in particular for cases wherein electrical power is available in surplus, especially for heating one or more of the feed streams or combined feed streams, in particular with a plasma torch or plasma arc. Thus, it is particularly possible to use a low O2input if green power or even a surplus of green power, is available for generating a comparatively high plasma fraction. If a lower amount of green power is available for generating a plasma, then the O2input can be increased.

[0017] Additionally, it has been found that the feedstocks used for the process for preparing syngas can be used without prior purification. Thus, in particular feedstocks comprising impurities can be used, which would have a detrimental effect on a pre-reformer.

[0018] Therefore, the present invention relates to a process for preparing syngas, the process comprising

[0019] (i) preparing a first feed stream comprising one or more organic compounds;

[0020] (ii) preparing a second feed stream comprising CO2and optionally comprising O2; (iii) optionally preparing a third feed stream comprising steam;

[0021] (iv) heating the second feed stream, or optionally combining and heating the first and second feed streams, or optionally combining and heating the second and third feed streams, or optionally combining and heating the first, second, and third feed streams, wherein the feed stream or the optionally combined feed streams are heated to a temperature in the range of from 1 ,000 to 20,000 °C;

[0022] (v) combining the heated second feed stream obtained in (iv) with the first feed stream and optionally with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined first and second feed streams obtained in (iv) with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined second and third feed streams obtained in (iv) with the first feed stream, obtaining a reaction stream;

[0023] (vi) feeding the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v) in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2and H2O, wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

[0024] It is preferred that in (iv) optional combining is performed prior to and / or during heating, more preferably prior to heating.

[0025] It is preferred that in (iv) the second feed stream is heated.

[0026] It is preferred that in (iv) the first and second feed streams are combined, obtaining a combined feed stream M1 2, and the combined feed stream M1 2is heated.

[0027] It is preferred that in (v) the combined and heated feed stream M1 2is combined with the third feed stream, obtaining a reaction stream.

[0028] In the case wherein in (v) the combined and heated feed stream M1 2is combined with the third feed stream, obtaining a reaction stream, it is preferred that in (vi) the heated feed stream M1 2obtained in (iv) is fed in the reaction zone.

[0029] It is preferred that in (iv) the second and third feed streams are combined, obtaining a combined feed stream M2 3, and the combined feed stream M2 3is heated.

[0030] In the case wherein in (iv) the second and third feed streams are combined, obtaining a combined feed stream M23, and the combined feed stream M23is heated, it is preferred that in (v) the combined and heated feed stream M23is combined with the first feed stream, obtaining a reaction stream. It is preferred that in (iv) the first, second, and third feed streams are combined, obtaining a combined feed stream M1-2’3, and the combined feed stream M1 2 3is heated.

[0031] In the case wherein in (iv) the first, second and third feed streams are combined, obtaining a combined feed stream M1 2 3, and the combined feed stream M1 2 3is heated, it is preferred that in (vi) the heated feed stream M1 2 3obtained in (iv) is fed in the reaction zone.

[0032] It is preferred that in (iv) the feed stream or the combined feed stream is heated to a temperature in the range of from 1 ,000 to 20,000°C, more preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0033] It is preferred that in (iv) the feed stream or the combined feed stream has a pressure in the range of from 0.1 to 80 bara, more preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably from 1 to 5 bara.

[0034] It is preferred that in (vi) the reaction stream according to any one of the embodiments disclosed hereinabove is fed in the reaction zone.

[0035] Furthermore and independently from the above, the present invention relates to an alternative process for preparing syngas, the process comprising

[0036] (i) preparing a first feed stream comprising one or more organic compounds;

[0037] (ii) preparing a second feed stream comprising CO2 and optionally comprising O2;

[0038] (iii) optionally preparing a third feed stream comprising steam;

[0039] (iv) heating the second feed stream, or heating the optional third feed stream, or heating the second feed stream and the optional third feed stream, wherein the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream are heated to a temperature in the range of from 1 ,000 to 20,000 °C;

[0040] (v) combining the first feed stream, the second feed stream, and the optional third feed stream, obtaining a reaction stream;

[0041] (vi) feeding the reaction stream in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2and H2O, wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

[0042] More specifically, and independently from the above, the present invention relates to an alternative process for preparing syngas, the process comprising

[0043] (i) preparing a first feed stream comprising one or more organic compounds;

[0044] (ii) preparing a second feed stream comprising CO2and optionally comprising O2;

[0045] (iii) optionally preparing a third feed stream comprising steam; (iv) heating the second feed stream, or heating the optional third feed stream, or heating the second feed stream and the optional third feed stream, wherein the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream are heated to a temperature in the range of from 1 ,000 to 20,000 °C;

[0046] (v) combining the first feed stream, the heated second feed stream, and the optional third feed stream, obtaining a reaction stream;

[0047] (vi) feeding the reaction stream in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2and H2O, wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

[0048] It is preferred according to the alternative process that the second feed stream is heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C, more preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0049] It is preferred according to the alternative process that the heated second feed stream has a pressure in the range of from 0.1 to 80 bara, more preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara.

[0050] It is preferred according to the alternative process that the optional third feed stream is heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C, more preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0051] It is preferred according to the alternative process that the heated optional third feed stream has a pressure in the range of from 0.1 to 80 bara, more preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara.

[0052] It is preferred according to the alternative process that, independently from one another, the second feed stream and the optional third feed stream are heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C, more preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0053] It is preferred according to the alternative process that, independently from one another, the heated second feed stream and the heated optional third feed stream have a pressure in the range of from 0.1 to 80 bara, more preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara. It is preferred according to the alternative process that the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream are heated in (iv) to a temperature in the range of from 1 ,100 to 4,000 °C, more preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0054] It is preferred according to the alternative process that the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream heated in (iv) have a pressure in the range of from 0.1 to 80 bara, more preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara.

[0055] It is preferred according to the alternative process that after (iii) and prior to (iv) the first feed stream and the second feed stream are combined, obtaining a combined feed stream M1 2, wherein in (iv) the optional third feed stream is heated to a temperature in the range of from 1 , 100 to 4,000 °C, more preferably to a temperature in the range of from 1 , 100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C, and wherein combining in (v) comprises combining the combined feed stream M1 2and the heated optional third feed stream.

[0056] It is preferred according to the alternative process that after (iii) and prior to (iv) the first feed stream and the optional third feed stream are combined, obtaining a combined feed stream M1 3, wherein in (iv) the second feed stream is heated to a temperature in the range of from 1 ,100 to 4,000 °C, more preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C, and wherein combining in (v) comprises combining the combined feed stream M1 3and the heated second stream.

[0057] It is preferred according to the alternative process that after (iii) and prior to (iv) the second feed stream and the optional third feed are combined, obtaining a combined feed stream M2 3, wherein in (iv) the combined feed stream M2 3comprising the second feed stream and the optional third stream are heated to a temperature in the range of from 1 ,100 to 4,000 °C, more preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C, and wherein combining in (v) comprises combining the heated combined feed stream M2 3and the first feed stream.

[0058] It is preferred according to the alternative process that combining in (v) is performed by injecting the first feed stream in one or both of the second feed stream and the optional third feed stream, wherein combining in (v) is optionally performed by spraying of the first feed stream with one or both of the second feed stream and the optional third feed stream. It is preferred according to the alternative process that in (v) the heated second feed stream obtained in (iv) is combined with the first feed stream, obtaining a reaction stream.

[0059] It is preferred according to the alternative process that in (v) the heated second feed stream obtained in (iv) is combined with the first and third feed streams, obtaining a reaction stream.

[0060] It is preferred that from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the one or more organic compounds comprised in the first feed stream prepared in (i) consist of C, H, and optionally one or more of O, S, and N.

[0061] It is preferred that from 49.5 to 100 weight-%, more preferably from 60 to 90 weight-%, more preferably from 70 to 80 weight-%, of the one or more organic compounds consist of C.

[0062] It is preferred that from 0.5 to 12 weight-%, more preferably from 2 to 10 weight-%, more preferably from 4 to 8 weight-%, of the one or more organic compounds consist of H.

[0063] It is preferred that from 0 to 50 weight-%, more preferably from 10 to 40 weight-%, more preferably from 20 to 30 weight-%, of the one or more organic compounds consist of O.

[0064] It is preferred that from 0 to 10 weight-%, more preferably from 2 to 8 weight-%, more preferably from 4 to 6 weight-%, of the one or more organic compounds consist of S.

[0065] It is preferred that from 0 to 10 weight-%, more preferably from 2 to 8 weight-%, more preferably from 4 to 6 weight-%, of the one or more organic compounds consist of N.

[0066] It is preferred that the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of CH4, C2H6, C3H8, C4H10, and mixtures of two or more thereof, wherein the one or more organic compounds preferably are CH4.

[0067] It is preferred that the one or more organic compounds comprise one or more organic compounds which are in the liquid phase under standard pressure and temperature, and one or more organic compounds which are in the solid phase under standard pressure and temperature, wherein preferably the solid phase is homogeneously distributed within the liquid phase.

[0068] It is preferred that the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of pyrolysis oils, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 as- phalthene fraction, preferably C5 asphalthene, high viscous residues, bio oils, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, polyamide particles, and mixtures thereof, wherein the one or more compounds more preferably are pyrolysis oils. In the case wherein the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of pyrolysis oils, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 as- phalthene fraction, preferably C5 asphalthene, high viscous residues, bio oils, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, polyamide particles, and mixtures thereof, it is preferred that the pyrolysis oils are preferably obtained from pyrolysis of one or more of biomass, plastic waste, and mixed plastic waste, preferably mixed plastic waste, wherein the mixed plastic waste preferably comprises optionally shredded waste tires, wherein the mixed plastic waste more preferably comprises one or more of polyethylenes, polypropylenes, polyisoprenes, polyethylene terephthalates, polystyrenes, copolymers of one or more thereof, block polymers of one or more thereof, graft copolymers of one or more thereof, and mixtures of two or more thereof.

[0069] Further in the case wherein the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of pyrolysis oils, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, preferably C5 asphalthene, high viscous residues, bio oils, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, polyamide particles, and mixtures thereof, it is preferred that the heating oils have a boiling point in the range of from 100 to 1 ,000 °C, more preferably in the range of from 150 to 750 °C, more preferably in the range of from 200 to 500 °C, more preferably in the range of from 225 to 375 °C, more preferably in the range of from 250 to 350 °C, preferably at a pressure in the range of from 0.99 to 1.01 bara.

[0070] It is preferred that the one or more organic compounds have a lower heating value in the range of from 10 to 60 MJ / kg, more preferably in the range of from 30 to 50 MJ / kg.

[0071] It is preferred that the one or more organic compounds have a viscosity in the range of from 20 to 6,000 mPas, more preferably in the range of from 100 to 5,000 mPas, wherein the viscosity is preferably determined according to Reference Example 1 .

[0072] It is preferred that from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 97 to 100 weight-%, more preferably from 99 to 100 weight-%, of the first feed stream prepared in (i) consist of the one or more organic compounds.

[0073] It is preferred that the first feed stream prepared in (i) comprises from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of O2.

[0074] It is preferred that the first feed stream prepared in (i) comprises from 0 to 50 weight-%, more preferably from 0 to 40 weight-%, more preferably from 0 to 30 weight-%, more preferably from 0 to 20 weight-%, more preferably from 0 to 15 weight-%, more preferably from 0 to 10 weight- %, more preferably from 0 to 5 weight-%, more preferably from 0 to 1 .6 weight-%, more preferably from 0 to 1 .5 weight-%, of CO2.

[0075] It is preferred that the first feed stream prepared in (i) has a temperature in the range of from 30 to 100 °C, more preferably in the range of from 50 to 80 °C, more preferably in the range of from 60 to 70 °C.

[0076] It is preferred that the first feed stream prepared in (i) has a pressure in the range of from 5 to 80 bara, more preferably in the range of from 35 to 70 bara, more preferably in the range of from 45 to 60 bara.

[0077] It is preferred that the first feed stream prepared in (i) has a mass flow rate in the range of from 100 to 20,000 kg / h, more preferably in the range of from 3,000 to 17,000 kg / h, more preferably in the range of from 5,000 to 15,000 kg / h, more preferably in the range of from 7,000 to 13,000 kg / h.

[0078] It is preferred that the first feed stream prepared in (i) comprises from 0 to 5 weight-%, more preferably from 0 to 3 weight-%, more preferably from 0 to 1 weight-%, more preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.05 weight- %, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of N2.

[0079] It is preferred that from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the second feed stream prepared in (ii) consist of CO2.

[0080] It is preferred according to a first alternative that the second feed stream prepared in (ii) comprises from 10 to 70 weight-%, more preferably from 15 to 65 weight-%, more preferably from 20 to 60 weight-%, more preferably from 25 to 55 weight-%, more preferably from 30 to 50 weight-%, more preferably from 35 to 45 weight-%, of O2.

[0081] It is preferred according to a second alternative that the second feed stream prepared in (ii) comprises from 0 to 10 weight-%, more preferably from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of O2.

[0082] It is preferred that the second feed stream prepared in (ii) comprises from 0 to 50 weight-%, more preferably from 0 to 30 weight-%, more preferably from 0 to 10 weight-%, more preferably from 0 to 5 weight-%, more preferably from 0 to 3 weight-%, more preferably from 0 to 1 weight- %, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of N2.

[0083] It is preferred that the second feed stream prepared in (ii) comprises from 0 to 5 weight-%, more preferably from 0 to 3 weight-%, more preferably from 0 to 1 weight-%, more preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.05 weight- %, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of N2.

[0084] It is preferred that the second feed stream prepared in (ii) has a temperature in the range of from 10 to 150 °C, more preferably in the range of from 15 to 75 °C, more preferably in the range of from 20 to 40 °C.

[0085] It is preferred that the second feed stream prepared in (ii) has a pressure in the range of from 0.1 to 10 bara, more preferably in the range of from 0.5 to 5 bara, more preferably in the range of from 0.8 to 1 .2 bara.

[0086] It is preferred that the second feed stream prepared in (ii) has a mass flow rate in the range of from 1 to 1000 kg / h, more preferably in the range of from 50 to 800 kg / h, more preferably in the range of from 100 to 600 kg / h.

[0087] It is preferred that the process comprises preparing a third feed stream comprising steam in (iii).

[0088] In the case wherein the process comprises preparing a third feed stream comprising steam in (iii), it is preferred that from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the third feed stream prepared in (iii) consist of steam.

[0089] Further in the case wherein the process comprises preparing a third feed stream comprising steam in (iii), it is preferred that the third feed stream prepared in (iii) comprises from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of O2.

[0090] Further in the case wherein the process comprises preparing a third feed stream comprising steam in (iii), it is preferred that the third feed stream prepared in (iii) has a temperature in the range of from 100 to 500 °C, more preferably in the range of from 200 to 400 °C, more preferably in the range of from 250 to 360 °C.

[0091] Further in the case wherein the process comprises preparing a third feed stream comprising steam in (iii), it is preferred that the third feed stream prepared in (iii) has a pressure in the range of from 5 to 100 bara, more preferably in the range of from 45 to 85 bara, more preferably in the range of from 60 to 75 bara.

[0092] Further in the case wherein the process comprises preparing a third feed stream comprising steam in (iii), it is preferred that the third feed stream prepared in (iii) has a mass flow rate in the range of from 5 to 5,000 kg / h, more preferably in the range of from 35 to 1 ,000 kg / h, more preferably in the range of from 40 to 165 kg / h.

[0093] It is preferred that heating in (iv) is directly or indirectly achieved by means of electricity, wherein preferably heating in (iv) is achieved by electrically generated or electrically induced plasma. It is preferred that heating in (iv) is achieved by one or more heating means, more preferably by one or more plasma generating means, wherein the plasma generating means is preferably selected from the group consisting of a plasma torch and a plasma arc, wherein more preferably heating in (iv) is achieved by 1 to 20, preferably by 2 to 10, more preferably by 4 to 6, plasma generating means.

[0094] In the case wherein heating in (iv) is achieved by one or more plasma generating means, wherein a plasma generating means is preferably selected from the group consisting of a plasma torch and a plasma arc, it is preferred that the plasma torch is transferred or non-trans- ferred, preferably non-transferred.

[0095] Further in the case wherein heating in (iv) is achieved by one or more plasma generating means, wherein a plasma generating means is preferably selected from the group consisting of a plasma torch and a plasma arc, it is preferred that the plasma torch is operated at a pressure of from 0.1 to 80 bara, more preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably from 1 to 5 bara.

[0096] It is preferred that in (iv) heating the second feed stream, heating the optional third feed stream, heating the second feed stream and the optional third feed stream, heating the first and second feed streams, heating the second and third feed streams, or heating the first, second, and third feed streams comprises irradiating the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams with microwaves as the heating means.

[0097] In the case wherein in (iv) heating the second feed stream, heating the optional third feed stream, heating the second feed stream and the optional third feed stream, heating the first and second feed streams, heating the second and third feed streams, or heating the first, second, and third feed streams comprises irradiating the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams with microwaves, it is preferred that the microwaves have a wavelength in the range of from 30 cm to 1 mm.

[0098] Further in the case wherein in (iv) heating the second feed stream, heating the optional third feed stream, heating the second feed stream and the optional third feed stream, heating the first and second feed streams, heating the second and third feed streams, or heating the first, second, and third feed streams comprises irradiating the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams with microwaves, it is preferred that the microwaves have a frequency in the range of from 1 to 300 GHz. the case wherein in (iv) heating the second feed stream, heating the optional third feed stream, heating the second feed stream and the optional third feed stream, heating the first and second feed streams, heating the second and third feed streams, or heating the first, second, and third feed streams comprises irradiating the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams with microwaves, it is preferred that the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams are irradiated with microwaves, preferably for generating a plasma. the case wherein in (iv) heating the second feed stream, heating the optional third feed stream, heating the second feed stream and the optional third feed stream, heating the first and second feed streams, heating the second and third feed streams, or heating the first, second, and third feed streams comprises irradiating the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams with microwaves, it is preferred that the total power output of the one or more heating means, more preferably of the one or more plasma generating means, is in the range of from 100 to 100,000 kW, preferably in the range of from 200 to 75,000 kW, more preferably in the range of from 300 to 50,000 kW, more preferably in the range of from 400 to 25,000 kW, more preferably in the range of from 500 to 10,000 kW, more preferably in the range of from 600 to 5,000 kW, more preferably in the range of from 700 to 4,000 kW, more preferably in the range of from 800 to 3,000 kW, more preferably in the range of from 900 to 2,800 kW, more preferably in the range of from 1 ,000 to 2,700 kW.

[0099] It is preferred that combining in (iv) or (v) is performed in a mixing chamber.

[0100] It is preferred that the reaction stream obtained from (v) displays a multiphase flow regime, more preferably a two phase flow regime.

[0101] It is preferred that the reaction stream obtained from (v) displays a dispersed flow regime, a plug flow regime, a slug flow regime, a wavy flow regime, a stratified flow regime, an annular flow regime or a mist flow regime, preferably a dispersed flow regime, wherein the reaction stream obtained from (v) preferably displays a horizontal flow.

[0102] It is preferred that the reaction stream obtained from (v) displays a churn flow regime, an annular flow regime, or a wispy annular flow regime, preferably an annular flow regime, wherein the reaction stream obtained from (v) preferably displays a vertical flow. It is preferred that the reaction stream obtained in (v) has a molar ratio, n(O):n(C), of oxygen, calculated as atomic oxygen, to carbon, calculated as elemental carbon, in the range of from 0.50:1 to 1.75:1 , more preferably in the range of from 0.75:1 to 1.50:1 , more preferably in the range of from 0.97:1 to 1.23:1.

[0103] It is preferred that the reaction stream obtained in (v) has a molar ratio, n(H):n(C), of hydrogen, calculated as atomic hydrogen, to carbon, calculated as elemental carbon, in the range of from 0.50:1 to 5.75:1 , more preferably in the range of from 1.75:1 to 5.00:1 , more preferably in the range of from 2.10:1 to 4.24: 1 .

[0104] It is preferred that the reaction stream obtained in (v) has a molar ratio, n(O):n(H), of oxygen, calculated as atomic oxygen, to hydrogen, calculated as atomic hydrogen, in the range of from 0.05:1 to 1.00:1 , more preferably in the range of from 0.17:1 to 0.60:1 , more preferably in the range of from 0.24:1 to 0.52:1.

[0105] It is preferred that the reaction stream obtained in (v) has a molar ratio, n(O):n(C):n(H), of oxygen, calculated as atomic oxygen, to carbon, calculated as elemental carbon, to hydrogen, calculated as atomic hydrogen, in the range of from 0.50:1 :0.50 to 1.75:1 :5.75, more preferably in the range of from 0.75:1 :1 .75 to 1 .50:1 :5.00, more preferably in the range of from 0.97:1 :2.10 to 1.23:1 :4.24.

[0106] It is preferred that the reaction zone is comprised in a reactor.

[0107] It is preferred that the maximum temperature of the reaction zone in (vi) is in the range of from 900 to 1 ,700 °C, more preferably in the range of from 1 ,200 to 1 ,500 °C, more preferably in the range of from 1 ,300 to 1 ,400 °C.

[0108] It is preferred that in the reaction zone in (vi) the reaction stream has a pressure in the range of from 1 to 100 bara, more preferably in the range of from 25 to 75 bara, more preferably in the range of from 40 to 50 bara.

[0109] It is preferred that in the reaction zone in (vi) the reaction stream is reacted by gasification, more preferably entrained flow gasification (German “Flugstromvergasung”).

[0110] It is preferred that the reaction zone comprises from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, based on 100 weight-% of the material comprised in the reaction zone, of a catalytically active metal M selected from the group consisting of Ni, Ce, Zr, Mg, Cr, Al, and mixtures of two or more thereof, preferably of a catalytically active metal M selected from groups 2 to 13, more preferably of a catalytically active material effective for converting an organic compound and an oxygen-containing compound to CO and H2.

[0111] It is preferred that E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combus- tion)) and the energy provided for heating in (iv) (E(heating)) according to formula I:

[0112] E(thermal) = E(combustion) + E(heating) (I) wherein E(thermal) is comprised in the range of from 4 to 360 MJ per kg of the one or more organic compounds comprised in the first feed stream, preferably from 18 to 180 MJ per kg, more preferably from 36 to 72 MJ per kg, and more preferably 50 to 54 MJ per kg of the one or more organic compounds comprised in the first feed stream, wherein E(combustion) is comprised in the range of from 0 to 356 MJ per kg of the one or more organic compounds comprised in the first feed stream, preferably from 0 to 176 MJ per kg, more preferably from 0 to 68 MJ per kg, and more preferably 0 to 50 MJ per kg of the one or more organic compounds comprised in the first feed stream, and wherein E(heating) is comprised in the range of from 4 to 360 MJ per kg of the one or more organic compounds comprised in the first feed stream, preferably from 4 to 180 MJ per kg, more preferably from 4 to 72 MJ per kg, and more preferably 4 to 54 MJ per kg of the one or more organic compounds comprised in the first feed stream.

[0113] In the case wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combus- tion)) and the energy provided for heating in (iv) (E(heating)) according to formula I as defined hereinabove, it is preferred that the amount of O2 comprised in the second feed stream is varied, such that the amount of O2 comprised in the second feed stream varies between 0 and 10.5 kg per kg of the one or more organic compounds comprised in the first feed stream, more preferably between 0 to 8 kg per kg, more preferably between 0 to 5 kg per kg, more preferably between 0 to 3 kg per kg, more preferably between 0 to 1 .40 kg per kg, and more preferably between 0 to 1 .06 kg per kg of the one or more organic compounds comprised in the first feed stream.

[0114] In the case wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combus- tion)) and the energy provided for heating in (iv) (E(heating)) according to formula I as defined hereinabove, it is preferred that preferably the amount of O2 comprised in the second feed stream is varied, such that upon combining of the first and second feed streams in (iv) or (v), the amount of O2 comprised in the second feed stream varies between 0 and 10.5 kg per kg of the one or more organic compounds comprised in the first feed stream, more preferably between 0 to 8 kg per kg, more preferably between 0 to 5 kg per kg, more preferably between 0 to 3 kg per kg, more preferably between 0 to 1 .40 kg per kg, and more preferably between 0 to 1 .06 kg per kg of the one or more organic compounds comprised in the first feed stream. In the case wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combus- tion)) and the energy provided for heating in (iv) (E(heating)) according to formula I as defined hereinabove, it is preferred that the frequency of the variation is in the range of once per 1 h and once per 48 h, more preferably in the range of once per 2 h and once per 24 h, more preferably in the range of once per 4 h and once per 8 h.

[0115] Within the meaning of the invention, the terms “varied" and “variation” indicate that the values in question are changed such that all of the values are traversed once when varying the values from the lowest value of the range to the highest value of the range or from the highest value of the range to the lowest value of the range, wherein the values lying in between the lowest value and the highest value may be traversed more than once during one variation.

[0116] In the case wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combus- tion)) and the energy provided for heating in (iv) (E(heating)) according to formula I as defined hereinabove, it is preferred that E(combustion) corresponds to the lower heating value of the one or more organic compounds comprised in the first feed stream, wherein E(combustion) more preferably corresponds to the lower heating value of the one or more organic compounds comprised in the first feed stream upon combining of the first and second feed streams in (iv) or (v), wherein the lower heating value is preferably determined according to ISO 6976:2016 and / or DIN 51900.

[0117] In the case wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combus- tion)) and the energy provided for heating in (iv) (E(heating)) according to formula I as defined hereinabove, it is preferred that E(heating) is the external energy provided for heating in (iv).

[0118] Within the meaning of the present invention, the term „external energy" refers to the energy provided from an external source of energy and which is used for heating in (iv), and which accordingly does not stem from chemical reaction which may take place between the components comprised in the optionally combined feed streams, or from any other interaction between the components comprised in the optionally combined feed streams which may lead to the release of thermal energy.

[0119] Within the meaning of the present invention, the term E(combustion) preferably refers to the energy obtained from partial and / or complete oxidation of the one or more organic compounds with O2. The process of any one of embodiments 1 to 90, wherein the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v), comprises a mass flow rate of O2 in the range of from 0 to 20,000 kg / h, preferably in the range of from 0 to 17,000 kg / h, more preferably in the range of from 0 to 15,000 kg / h, more preferably in the range of from O to 14,000 kg / h.

[0120] It is preferred that the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v), comprises a mass flow rate of the one or more organic compounds in the range of from 100 to 20,000 kg / h, more preferably in the range of from 3,000 to 17,000 kg / h, more preferably in the range of from 5,000 to 15,000 kg / h, more preferably in the range of from 6,000 to 14,000 kg / h.

[0121] It is preferred that the product stream comprises a molar ratio, H2:CO, of H2 to CO in the range of from 0.3:1 to 3.7:1 , more preferably in the range of from 0.4:1 to 3.6:1 , more preferably in the range of from 0.5:1 to 3.5:1 , more preferably in the range of from 0.6:1 to 3.4:1 , more preferably in the range of from 0.7:1 to 3.3:1 , more preferably in the range of from 0.8:1 to 3.2:1 , more preferably in the range of from 0.9:1 to 3.1 :1 , more preferably in the range of from 1 :1 to 3:1.

[0122] It is preferred that the process further comprises after (vi)

[0123] (vii) separating CO2 from the product stream obtained in (vi), obtaining a stream comprising CO2 and a product stream being CO2 depleted.

[0124] In the case wherein the process further comprises (vii), it is preferred that separating CO2is performed by a CO2scrubber or by CO2absorption.

[0125] Further in the case wherein the process further comprises (vii), it is preferred that the process further comprises after (vii)

[0126] (viii) compressing the stream comprising CO2 obtained from (vii), more preferably to a stream having a pressure in the range of from 0.1 to 100 bara, preferably in the range of from 0.5 to 80 bara, more preferably in the range of from 0.8 to 60 bara, more preferably in the range of from 25 to 55 bara, more preferably in the range of from 45 to 55 bara.

[0127] It is preferred according to a first alternative that the process further comprises after (vi), preferably after (vii), more preferably after (viii),

[0128] (ix) recycling at least a portion of the stream comprising CO2 obtained from (vii) or (viii) into the second feed stream prepared in (ii), more preferably recycling the stream comprising CO2 obtained from (vii) or (viii) into the second feed stream prepared in (ii).

[0129] In the case wherein the process further comprises (ix), it is preferred that from 1 to 100 weight- %, more preferably from 3 to 99 weight-%, more preferably from 5 to 98 weight-%, more preferably from 10 to 95 weight-%, more preferably from 15 to 90 weight-%, more preferably from 20 to 80 weight-%, more preferably from 25 to 75 weight-%, more preferably from 40 to 60 weight- %, of the second feed stream prepared in (II) consist of the stream comprising CO2obtained from (vii) or (viii).

[0130] It is preferred according to a second alternative that the process further comprises after (vi), preferably after (vii), more preferably after (viii),

[0131] (ix’) recycling at least a portion of the stream comprising CO2obtained from (vii) or (viii) into the second feed stream prepared in (ii), more preferably recycling the stream comprising CO2obtained from (vii) or (viii) into the second feed stream prepared in (ii), wherein the weight ratio of CO2recycled to the second feed stream to the CO2comprised in the second feed stream prepared in (ii) is in the range of from 1 :1 to 5:1 , preferably in the range of from 1 :1 to 2:1 , more preferably in the range of from 1 :1 to 1.5:1.

[0132] In the case wherein the process further comprises (ix’), it is preferred that from 1 to 100 weight- %, more preferably from 25 to 75 weight-%, more preferably from 40 to 60 weight-%, of the CO2recycled to the second feed stream obtained from (ix’) consists of recycled CO2from the stream comprising CO2obtained in (vii) or (viii).

[0133] It is preferred that the process further comprises after (vi), preferably after (viii), more preferably after (ix),

[0134] (x) adding H2to the product stream obtained from (vi) or to the product stream being CO2depleted obtained from (vii).

[0135] In the case wherein the process further comprises (x), it is preferred H2added to the product stream obtained from (vi) or to the product stream being CO2depleted obtained from (vii) comprises one or more of H2obtained from a pipeline, H2obtained from a tank, H2obtained from a different process, more preferably from a process for preparing styrene, and H2obtained from electrolysis, preferably from electrolysis using green power.

[0136] It is preferred that the molar ratio of CO2comprised in the product stream obtained in (vi) to CO2comprised in the reaction stream obtained in (v) is less than 1 :1.

[0137] It is preferred that the product stream obtained from (vi) or the product stream being CO2depleted obtained from (vii) has a volume ratio, H2:CO2, of H2to CO in the range of from 0.9:1 to 2.9:1 , more preferably in the range of from 1.3:1 to 2.5:1 , more preferably in the range of from 1 .7:1 to 2.1 :1 , wherein the product stream obtained from (vi) or the product stream being CO2depleted obtained from (vii) more preferably has a volume ratio, H2:CO2, of H2to CO of 1.8:1.

[0138] The invention further relates to a process, preferably according to the process described herein, comprising the step:

[0139] - converting the product stream comprising H2and CO obtainable by or obtained by the process as described herein or a chemical material obtainable by or obtained by the process as described herein to obtain a monomer, polymer or polymer product. In a preferred embodiment, the monomer is a di- or polyol, preferably butandiol, aldehyde, preferably formaldehyde, di- or polyisocyanate, preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (IPDI), amide, preferably caprolactam, alkene, preferably styrene, ethene and norbornene, alkyne, (di)ester, preferably methyl methacrylate, mono or diacid, preferably adipic acid or terephthalic acid, diamine, preferably hexamethylenediamine, nonanediamine, or sulfones, preferably 4, 4'-dichlorodiphenyl sulfone.

[0140] In a preferred embodiment, the polymer is and / or the polymer product comprises polyamide (PA), preferably PA 6 or PA 66, polyisocyanate polyaddition product, preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR), low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (PTFE), poly(methyl acrylate) (PM A), poly(methyl methacrylate) (PM MA), polybutadiene (BR, PBD), poly(cis-1 ,4-isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate co-terephthalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PH A), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymer or mixture thereof.

[0141] In a preferred embodiment, the polymer and / or the polymer product is / are or is / are a part of:

[0142] - a part of a car, preferably cylinder head cover, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing, housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part, part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, cushion, or coating;

[0143] - a cloth, preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket;

[0144] - an electrical part, preferably electrical or electronic passive or active component, circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, microswitch, microbutton, semiconductor, reflector housing for light-emitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hook (snap- in), or spring tongue; - a consumer, agricultural product or pharmaceutical product, preferably tennis string, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion, insulation, detergent, dishwasher tabs or powder, shampoo, body wash, shower gel, soap, fertilizer, fungicide, or pesticide;

[0145] - a packaging for the food industry, preferably mono- or multi-layer blown film, cast film (mono- or multi-layer), biaxially stretched film, or laminating film; or

[0146] - a part of a construction, preferably a rotor blade, insulating material, frame, housing, wall, coating, or separating wall.

[0147] In a preferred embodiment, the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product 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.

[0148] In another preferred embodiment, the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight- % or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the feedstock in the product stream comprising H2and CO, monomer, polymer or polymer product 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 embodiment chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard; wherein the feedstock comprises, preferably consists of, the sum of the afore-mentioned feed streams including the first feed stream comprising one or more organic compounds, the second feed stream comprising CO2and optionally comprising O2and the third feed stream comprising steam.

[0149] The feedstock more preferably comprises, more preferably consists of, the sum of the aforementioned feed streams including the first feed stream comprising one or more organic compounds, the second feed stream comprising CO2and optionally comprising O2and the third feed stream comprising steam. Even more preferably the feedstock comprises, more preferably consists of the parts of the first feed stream comprising one or more organic compounds, the second feed stream comprising CO2and optionally comprising O2and the third feed stream comprising steam in the product stream comprising CO and H2.

[0150] The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any one of embodiments 1 to 4", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "The process of any one of embodiments 1 , 2, 3 and 4". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.

[0151] 1 . Process for preparing syngas, the process comprising

[0152] (i) preparing a first feed stream comprising one or more organic compounds;

[0153] (ii) preparing a second feed stream comprising CO2and optionally comprising O2;

[0154] (iii) optionally preparing a third feed stream comprising steam;

[0155] (iv) heating the second feed stream, or optionally combining and heating the first and second feed streams, or optionally combining and heating the second and third feed streams, or optionally combining and heating the first, second, and third feed streams, wherein the feed stream or the optionally combined feed streams are heated to a temperature in the range of from 1 ,000 to 20,000 °C;

[0156] (v) combining the heated second feed stream obtained in (iv) with the first feed stream and optionally with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined first and second feed streams obtained in (iv) with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined second and third feed streams obtained in (iv) with the first feed stream, obtaining a reaction stream;

[0157] (vi) feeding the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v) in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2and H2O, wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

[0158] 2. The process of embodiment 1 , wherein in (iv) optional combining is performed prior to and / or during heating, preferably prior to heating.

[0159] 3. The process of embodiment 1 or 2, wherein in (iv) the second feed stream is heated.

[0160] 4. The process of embodiment 1 or 2, wherein in (iv) the first and second feed streams are combined, obtaining a combined feed stream M1 2, and the combined feed stream M1 2is heated.

[0161] 5. The process of embodiment 4, wherein in (v) the combined and heated feed stream M1 2is combined with the third feed stream, obtaining a reaction stream.

[0162] 6. The process of embodiment 4, wherein in (vi) the heated feed stream M1 2obtained in (iv) is fed in the reaction zone.

[0163] 7. The process of embodiment 1 or 2, wherein in (iv) the second and third feed streams are combined, obtaining a combined feed stream M2 3, and the combined feed stream M2 3is heated.

[0164] 8. The process of embodiment 7, wherein in (v) the combined and heated feed stream M2 3is combined with the first feed stream, obtaining a reaction stream.

[0165] 9. The process of embodiment 1 or 2, wherein in (iv) the first, second, and third feed streams are combined, obtaining a combined feed stream M1-2’3, and the combined feed stream M1-2’3is heated.

[0166] 10. The process of embodiment 9, wherein in (vi) the heated feed stream M1’2’3obtained in (iv) is fed in the reaction zone.

[0167] 11 . The process of any one of embodiments 1 to 10, wherein in (iv) the feed stream or the combined feed stream is heated to a temperature in the range of from 1 ,000 to 20,000°C, preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0168] 12. The process of any one of embodiments 1 to 11 , wherein in (iv) the feed stream or the combined feed stream has a pressure in the range of from 0.1 to 80 bara, preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably from 1 to 5 bara. 13. The process of any one of embodiments 1 to 12, wherein in (vi) the reaction stream according to any one of embodiments 1 to 12 is fed in the reaction zone.

[0169] 14. Process for preparing syngas, the process comprising

[0170] (i) preparing a first feed stream comprising one or more organic compounds;

[0171] (ii) preparing a second feed stream comprising CO2 and optionally comprising O2;

[0172] (iii) optionally preparing a third feed stream comprising steam;

[0173] (iv) heating the second feed stream, or heating the optional third feed stream, or heating the second feed stream and the optional third feed stream, wherein the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream are heated to a temperature in the range of from 1 ,000 to 20,000 °C;

[0174] (v) combining the first feed stream, the second feed stream, and the optional third feed stream, obtaining a reaction stream;

[0175] (vi) feeding the reaction stream in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2and H2O, wherein the one or more organic compounds independently from one another comprise C,

[0176] H, and optionally one or more of O, S, and N.

[0177] 15. The process of embodiment 14, wherein the second feed stream is heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C, preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0178] 16. The process of embodiment 14 or 15, wherein the heated second feed stream has a pressure in the range of from 0.1 to 80 bara, preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara.

[0179] 17. The process of any one of embodiments 14 to 16, wherein the optional third feed stream is heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C, preferably from

[0180] I ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0181] 18. The process of any one of embodiments 14 to 17, wherein the heated optional third feed stream has a pressure in the range of from 0.1 to 80 bara, preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara. 19. The process of any one of embodiments 14 to 18, wherein, independently from one another, the second feed stream and the optional third feed stream are heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C, preferably from 1 ,100 to 4,000 °C, more preferably from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0182] 20. The process of any one of embodiments 14 to 19, wherein, independently from one another, the heated second feed stream and the heated optional third feed stream have a pressure in the range of from 0.1 to 80 bara, preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara.

[0183] 21 . The process of any one of embodiments 14 to 20, wherein the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream are heated in (iv) to a temperature in the range of from 1 ,100 to 4,000 °C, preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C.

[0184] 22. The process of any one of embodiments 14 to 21 , wherein the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream heated in (iv) have a pressure in the range of from 0.1 to 80 bara, preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably in the range of from 1 to 5 bara.

[0185] 23. The process of any one of embodiments 14 to 22, wherein after (iii) and prior to (iv) the first feed stream and the second feed stream are combined, obtaining a combined feed stream M1 2, wherein in (iv) the optional third feed stream is heated to a temperature in the range of from 1 ,100 to 4,000 °C, preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C, and wherein combining in (v) comprises combining the combined feed stream M1 2and the heated optional third feed stream.

[0186] 24. The process of any one of embodiments 14 to 23, wherein after (iii) and prior to (iv) the first feed stream and the optional third feed stream are combined, obtaining a combined feed stream M1 3, wherein in (iv) the second feed stream is heated to a temperature in the range of from 1 ,100 to 4,000 °C, preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C, and wherein combining in (v) comprises combining the combined feed stream M1 3and the heated second stream. 25. The process of any one of embodiments 14 to 24, wherein after (iii) and prior to (iv) the second feed stream and the optional third feed are combined, obtaining a combined feed stream M23, wherein in (iv) the combined feed stream M2 3comprising the second feed stream and the optional third stream are heated to a temperature in the range of from 1 ,100 to 4,000 °C, preferably to a temperature in the range of from 1 ,100 to 3,000 °C, more preferably from 1 ,200 to 2,000 °C, more preferably from 1 ,200 to 1 ,500 °C, more preferably from 1 ,300 to 1 ,400 °C, and wherein combining in (v) comprises combining the heated combined feed stream M23and the first feed stream.

[0187] 26. The process of any one of embodiments 14 to 25, wherein combining in (v) is performed by injecting the first feed stream in one or both of the second feed stream and the optional third feed stream, wherein combining in (v) is optionally performed by spraying of the first feed stream with one or both of the second feed stream and the optional third feed stream.

[0188] 27. The process of any one of embodiments 14 to 26, wherein in (v) the heated second feed stream obtained in (iv) is combined with the first feed stream, obtaining a reaction stream.

[0189] 28. The process of any one of embodiments 14 to 27, wherein in (v) the heated second feed stream obtained in (iv) is combined with the first and third feed streams, obtaining a reaction stream.

[0190] 29. The process of any one of embodiments 1 to 28, wherein from 90 to 100 weight-%, preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the one or more organic compounds comprised in the first feed stream prepared in (i) consist of C, H, and optionally one or more of O, S, and N.

[0191] 30. The process of any one of embodiments 1 to 29, wherein from 49.5 to 100 weight-%, preferably from 60 to 90 weight-%, more preferably from 70 to 80 weight-%, of the one or more organic compounds consist of C.

[0192] 31. The process of any one of embodiments 1 to 30, wherein from 0.5 to 12 weight-%, preferably from 2 to 10 weight-%, more preferably from 4 to 8 weight-%, of the one or more organic compounds consist of H.

[0193] 32. The process of any one of embodiments 1 to 31 , wherein from 0 to 50 weight-%, preferably from 10 to 40 weight-%, more preferably from 20 to 30 weight-%, of the one or more organic compounds consist of O.

[0194] 33. The process of any one of embodiments 1 to 32, wherein from 0 to 10 weight-%, preferably from 2 to 8 weight-%, more preferably from 4 to 6 weight-%, of the one or more organic compounds consist of S. 34. The process of any one of embodiments 1 to 33, wherein from 0 to 10 weight-%, preferably from 2 to 8 weight-%, more preferably from 4 to 6 weight-%, of the one or more organic compounds consist of N.

[0195] 35. The process of any one of embodiments 1 to 34, wherein the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of CH4, C2H6, C3H8, C4H10, and mixtures of two or more thereof, wherein the one or more organic compounds preferably are CH4.

[0196] 36. The process of any one of embodiments 1 to 35, wherein the one or more organic compounds comprise one or more organic compounds which are in the liquid phase under standard pressure and temperature, and one or more organic compounds which are in the solid phase under standard pressure and temperature, wherein preferably the solid phase is homogeneously distributed within the liquid phase.

[0197] 37. The process of any one of embodiments 1 to 36, wherein the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of pyrolysis oils, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, preferably C5 asphalthene, high viscous residues, bio oils, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, polyamide particles, and mixtures thereof, wherein the one or more compounds preferably are pyrolysis oils.

[0198] 38. The process of embodiment 37, wherein the pyrolysis oils are preferably obtained from pyrolysis of one or more of biomass, plastic waste, and mixed plastic waste, preferably mixed plastic waste, wherein the mixed plastic waste preferably comprises optionally shredded waste tires, wherein the mixed plastic waste more preferably comprises one or more of polyethylenes, polypropylenes, polyisoprenes, polyethylene terephthalates, polystyrenes, copolymers of one or more thereof, block polymers of one or more thereof, graft copolymers of one or more thereof, and mixtures of two or more thereof.

[0199] 39. The process of embodiment 37 or 38, wherein the heating oils have a boiling point in the range of from 100 to 1 ,000 °C, preferably in the range of from 150 to 750 °C, more preferably in the range of from 200 to 500 °C, more preferably in the range of from 225 to 375 °C, more preferably in the range of from 250 to 350 °C, preferably at a pressure in the range of from 0.99 to 1.01 bara.

[0200] 40. The process of any one of embodiments 1 to 39, wherein the one or more organic compounds have a lower heating value in the range of from 10 to 60 MJ / kg, preferably in the range of from 30 to 50 MJ / kg. 41 . The process of any one of embodiments 1 to 40, wherein the one or more organic compounds have a viscosity in the range of from 20 to 6,000 mPas, preferably in the range of from 100 to 5,000 mPas, wherein the viscosity is preferably determined according to Reference Example 1 .

[0201] 42. The process of any one of embodiments 1 to 41 , wherein preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 97 to 100 weight-%, more preferably from 99 to 100 weight-%, of the first feed stream prepared in (i) consist of the one or more organic compounds.

[0202] 43. The process of any one of embodiments 1 to 42, wherein the first feed stream prepared in (i) comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of O2.

[0203] 44. The process of any one of embodiments 1 to 43, wherein the first feed stream prepared in (i) comprises from 0 to 50 weight-%, more preferably from 0 to 40 weight-%, more preferably from 0 to 30 weight-%, more preferably from 0 to 20 weight-%, more preferably from 0 to 15 weight-%, more preferably from 0 to 10 weight-%, more preferably from 0 to 5 weight-%, more preferably from 0 to 1 .6 weight-%, more preferably from 0 to 1 .5 weight- %, of CO2.

[0204] 45. The process of any one of embodiments 1 to 44, wherein the first feed stream prepared in (i) has a temperature in the range of from 30 to 100 °C, preferably in the range of from 50 to 80 °C, more preferably in the range of from 60 to 70 °C.

[0205] 46. The process of any one of embodiments 1 to 45, wherein the first feed stream prepared in (i) has a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 70 bara, more preferably in the range of from 45 to 60 bara.

[0206] 47. The process of any one of embodiments 1 to 46, wherein the first feed stream prepared in (i) has a mass flow rate in the range of from 100 to 20,000 kg / h, preferably in the range of from 3,000 to 17,000 kg / h, more preferably in the range of from 5,000 to 15,000 kg / h, more preferably in the range of from 7,000 to 13,000 kg / h.

[0207] 48. The process of any one of embodiments 1 to 47, wherein the first feed stream prepared in (i) comprises from 0 to 5 weight-%, preferably from 0 to 3 weight-%, more preferably from 0 to 1 weight-%, more preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.05 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of N2. 49. The process of any one of embodiments 1 to 48, wherein from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the second feed stream prepared in (ii) consist of CO2.

[0208] 50. The process of any one of embodiments 1 to 49, wherein the second feed stream prepared in (ii) comprises from 10 to 70 weight-%, preferably from 15 to 65 weight-%, more preferably from 20 to 60 weight-%, more preferably from 25 to 55 weight-%, more preferably from 30 to 50 weight-%, more preferably from 35 to 45 weight-%, of O2.

[0209] 51 . The process of any one of embodiments 1 to 49, wherein the second feed stream prepared in (ii) comprises from 0 to 10 weight-%, preferably from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of O2.

[0210] 52. The process of any one of embodiments 1 to 51 , wherein the second feed stream prepared in (ii) comprises from 0 to 50 weight-%, preferably from 0 to 30 weight-%, more preferably from 0 to 10 weight-%, more preferably from 0 to 5 weight-%, more preferably from 0 to 3 weight-%, more preferably from 0 to 1 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of N2.

[0211] 53. The process of any one of embodiments 1 to 52, wherein the second feed stream prepared in (ii) comprises from 0 to 5 weight-%, preferably from 0 to 3 weight-%, more preferably from 0 to 1 weight-%, more preferably from 0 to 0.5 weight-%, more preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.05 weight-%, more preferably from 0 to 0.01 weight-%, more preferably from 0 to 0.005 weight-%, more preferably from 0 to 0.001 weight-%, of N2.

[0212] 54. The process of any one of embodiments 1 to 53, wherein the second feed stream prepared in (ii) has a temperature in the range of from 10 to 150 °C, preferably in the range of from 15 to 75 °C, more preferably in the range of from 20 to 40 °C.

[0213] 55. The process of any one of embodiments 1 to 54, wherein the second feed stream prepared in (ii) has a pressure in the range of from 0.1 to 10 bara, preferably in the range of from 0.5 to 5 bara, more preferably in the range of from 0.8 to 1.2 bara.

[0214] 56. The process of any one of embodiments 1 to 55, wherein the second feed stream prepared in (ii) has a mass flow rate in the range of from 1 to 1000 kg / h, preferably in the range of from 50 to 800 kg / h, more preferably in the range of from 100 to 600 kg / h.

[0215] 57. The process of any one of embodiments 1 to 56, wherein the process comprises preparing a third feed stream comprising steam in (iii). 58. The process of embodiment 57, wherein from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the third feed stream prepared in (iii) consist of steam.

[0216] 59. The process of embodiment 57 or 58, wherein the third feed stream prepared in (iii) comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, of O2.

[0217] 60. The process of any one of embodiments 57 to 59, wherein the third feed stream prepared in (iii) has a temperature in the range of from 100 to 500 °C, preferably in the range of from 200 to 400 °C, more preferably in the range of from 250 to 360 °C.

[0218] 61. The process of any one of embodiments 57 to 60, wherein the third feed stream prepared in (iii) has a pressure in the range of from 5 to 100 bara, preferably in the range of from 45 to 85 bara, more preferably in the range of from 60 to 75 bara.

[0219] 62. The process of any one of embodiments 57 to 61 , wherein the third feed stream prepared in (iii) has a mass flow rate in the range of from 5 to 5,000 kg / h, preferably in the range of from 35 to 1 ,000 kg / h, more preferably in the range of from 40 to 165 kg / h.

[0220] 63. The process of any one of embodiments 1 to 62, wherein heating in (iv) is directly or indirectly achieved by means of electricity, wherein preferably heating in (iv) is achieved by electrically generated or electrically induced plasma.

[0221] 64. The process of any one of embodiments 1 to 63, wherein heating in (iv) is achieved by one or more heating means, preferably by one or more plasma generating means, wherein the plasma generating means is preferably selected from the group consisting of a plasma torch and a plasma arc, wherein more preferably heating in (iv) is achieved by 1 to 20, preferably by 2 to 10, more preferably by 4 to 6, plasma generating means.

[0222] 65. The process of embodiment 64, wherein the plasma torch is transferred or non-trans- ferred, preferably non-transferred.

[0223] 66. The process of embodiments 64 or 65, wherein the plasma torch is operated at a pressure of from 0.1 to 80 bara, preferably from 0.5 to 60 bara, more preferably from 1 to 40 bara, more preferably from 1 to 30 bara, more preferably from 1 to 20 bara, more preferably from 1 to 10 bara, and more preferably from 1 to 5 bara.

[0224] 67. The process of any one of embodiments 1 to 66, wherein in (iv) heating the second feed stream, heating the optional third feed stream, heating the second feed stream and the optional third feed stream, heating the first and second feed streams, heating the second and third feed streams, or heating the first, second, and third feed streams comprises irradiating the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams with microwaves as the heating means.

[0225] 68. The process of embodiment 67, wherein the microwaves have a wavelength in the range of from 30 cm to 1 mm.

[0226] 69. The process of embodiment 67 or 68, wherein the microwaves have a frequency in the range of from 1 to 300 GHz.

[0227] 70. The process any one of embodiments 67 to 69, wherein the second feed stream, the optional third feed stream, the second feed stream and the optional third feed stream, the first and second feed streams, the second and third feed streams, or the first, second, and third feed streams are irradiated with microwaves, preferably for generating a plasma.

[0228] 71 . The process of any one of embodiments 67 to 70, wherein the total power output of the one or more heating means, preferably of the one or more plasma generating means, is in the range of from 100 to 100,000 kW, preferably in the range of from 200 to 75,000 kW, more preferably in the range of from 300 to 50,000 kW, more preferably in the range of from 400 to 25,000 kW, more preferably in the range of from 500 to 10,000 kW, more preferably in the range of from 600 to 5,000 kW, more preferably in the range of from 700 to 4,000 kW, more preferably in the range of from 800 to 3,000 kW, more preferably in the range of from 900 to 2,800 kW, more preferably in the range of from 1 ,000 to 2,700 kW.

[0229] 72. The process of any one of embodiments 1 to 71 , wherein combining in (iv) or (v) is performed in a mixing chamber.

[0230] 73. The process of any one of embodiments 1 to 72, wherein the reaction stream obtained from (v) displays a multiphase flow regime, preferably a two phase flow regime.

[0231] 74. The process of any one of embodiments 1 to 73, wherein the reaction stream obtained from (v) displays a dispersed flow regime, a plug flow regime, a slug flow regime, a wavy flow regime, a stratified flow regime, an annular flow regime or a mist flow regime, preferably a dispersed flow regime, wherein the reaction stream obtained from (v) preferably displays a horizontal flow.

[0232] 75. The process of any one of embodiments 1 to 73, wherein the reaction stream obtained from (v) displays a churn flow regime, an annular flow regime, or a wispy annular flow regime, preferably an annular flow regime, wherein the reaction stream obtained from (v) preferably displays a vertical flow. 76. The process of any one of embodiments 1 to 75, wherein the reaction stream obtained in (v) has a molar ratio, n(O):n(C), of oxygen, calculated as atomic oxygen, to carbon, calculated as elemental carbon, in the range of from 0.50:1 to 1 .75:1 , preferably in the range of from 0.75:1 to 1.50:1 , more preferably in the range of from 0.97:1 to 1.23:1.

[0233] 77. The process of any one of embodiments 1 to 76, wherein the reaction stream obtained in (v) has a molar ratio, n(H):n(C), of hydrogen, calculated as atomic hydrogen, to carbon, calculated as elemental carbon, in the range of from 0.50:1 to 5.75:1 , preferably in the range of from 1.75:1 to 5.00:1 , more preferably in the range of from 2.10:1 to 4.24:1.

[0234] 78. The process of any one of embodiments 1 to 77, wherein the reaction stream obtained in (v) has a molar ratio, n(O):n(H), of oxygen, calculated as atomic oxygen, to hydrogen, calculated as atomic hydrogen, in the range of from 0.05:1 to 1.00:1 , preferably in the range of from 0.17:1 to 0.60:1 , more preferably in the range of from 0.24:1 to 0.52:1.

[0235] 79. The process of any one of embodiments 1 to 78, wherein the reaction stream obtained in (v) has a molar ratio, n(O):n(C):n(H), of oxygen, calculated as atomic oxygen, to carbon, calculated as elemental carbon, to hydrogen, calculated as atomic hydrogen, in the range of from 0.50:1 :0.50 to 1.75:1 :5.75, preferably in the range of from 0.75:1 :1.75 to 1.50:1 :5.00, more preferably in the range of from 0.97:1 :2.10 to 1.23:1 :4.24.

[0236] 80. The process of any one of embodiments 1 to 79, wherein the reaction zone is comprised in a reactor.

[0237] 81 . The process of any one of embodiments 1 to 80, wherein the maximum temperature of the reaction zone in (vi) is in the range of from 900 to 1 ,700 °C, preferably in the range of from 1 ,200 to 1 ,500 °C, more preferably in the range of from 1 ,300 to 1 ,400 °C.

[0238] 82. The process of any one of embodiments 1 to 81 , wherein in the reaction zone in (vi) the reaction stream has a pressure in the range of from 1 to 100 bara, preferably in the range of from 25 to 75 bara, more preferably in the range of from 40 to 50 bara.

[0239] 83. The process of any one of embodiments 1 to 82, wherein in the reaction zone in (vi) the reaction stream is reacted by gasification, preferably entrained flow gasification (German “Flugstromvergasung”).

[0240] 84. The process of any one of embodiments 1 to 83, wherein the reaction zone comprises from 0 to 1 weight-%, preferably from 0 to 0.1 weight-%, more preferably from 0 to 0.01 weight-%, based on 100 weight-% of the material comprised in the reaction zone, of a catalytically active metal M selected from the group consisting of Ni, Ce, Zr, Mg, Cr, Al, and mixtures of two or more thereof, preferably of a catalytically active metal M selected from groups 2 to 13, more preferably of a catalytically active material effective for converting an organic compound and an oxygen-containing compound to CO and H2. 85. The process of any one of embodiments 1 to 84, wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combustion)) and the energy provided for heating in (iv) (E(heating)) according to formula I:

[0241] E(thermal) = E(combustion) + E(heating) (I) wherein E(thermal) is comprised in the range of from 4 to 360 MJ per kg of the one or more organic compounds comprised in the first feed stream, preferably from 18 to 180 MJ per kg, more preferably from 36 to 72 MJ per kg, and more preferably 50 to 54 MJ per kg of the one or more organic compounds comprised in the first feed stream, wherein E(combustion) is comprised in the range of from 0 to 356 MJ per kg of the one or more organic compounds comprised in the first feed stream, preferably from 0 to 176 MJ per kg, more preferably from 0 to 68 MJ per kg, and more preferably 0 to 50 MJ per kg of the one or more organic compounds comprised in the first feed stream, and wherein E(heating) is comprised in the range of from 4 to 360 MJ per kg of the one or more organic compounds comprised in the first feed stream, preferably from 4 to 180 MJ per kg, more preferably from 4 to 72 MJ per kg, and more preferably 4 to 54 MJ per kg of the one or more organic compounds comprised in the first feed stream.

[0242] 86. The process of embodiment 85, wherein the amount of O2 comprised in the second feed stream is varied, such that the amount of O2 comprised in the second feed stream varies between 0 and 10.5 kg per kg of the one or more organic compounds comprised in the first feed stream, preferably between 0 to 8 kg per kg, more preferably between 0 to 5 kg per kg, more preferably between 0 to 3 kg per kg, more preferably between 0 to 1 .40 kg per kg, and more preferably between 0 to 1 .06 kg per kg of the one or more organic compounds comprised in the first feed stream.

[0243] 87. The process of embodiment 85 or 86, wherein preferably the amount of O2 comprised in the second feed stream is varied, such that upon combining of the first and second feed streams in (iv) or (v), the amount of O2comprised in the second feed stream varies between 0 and 10.5 kg per kg of the one or more organic compounds comprised in the first feed stream, preferably between 0 to 8 kg per kg, more preferably between 0 to 5 kg per kg, more preferably between 0 to 3 kg per kg, more preferably between 0 to 1.40 kg per kg, and more preferably between 0 to 1 .06 kg per kg of the one or more organic compounds comprised in the first feed stream.

[0244] 88. The process of any one of embodiments 85 to 87, wherein the frequency of the variation is in the range of once per 1 h and once per 48 h, preferably in the range of once per 2 h and once per 24 h, more preferably in the range of once per 4 h and once per 8 h. 89. The process of any one of embodiments 85 to 88, wherein E(combustion) corresponds to the lower heating value of the one or more organic compounds comprised in the first feed stream, wherein E(combustion) preferably corresponds to the lower heating value of the one or more organic compounds comprised in the first feed stream upon combining of the first and second feed streams in (iv) or (v), wherein the lower heating value is preferably determined according to ISO 6976:2016 and / or DIN 51900.

[0245] 90. The process of any one of embodiments 85 to 89, wherein E(heating) is the external energy provided for heating in (iv).

[0246] 91 . The process of any one of embodiments 1 to 90, wherein the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v), comprises a mass flow rate of O2 in the range of from 0 to 20,000 kg / h, preferably in the range of from 0 to 17,000 kg / h, more preferably in the range of from 0 to 15,000 kg / h, more preferably in the range of from 0 to 14,000 kg / h.

[0247] 92. The process of any one of embodiments 1 to 91 , wherein the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v), comprises a mass flow rate of the one or more organic compounds in the range of from 100 to 20,000 kg / h, preferably in the range of from 3,000 to 17,000 kg / h, more preferably in the range of from 5,000 to 15,000 kg / h, more preferably in the range of from 6,000 to 14,000 kg / h.

[0248] 93. The process of any one of embodiments 1 to 92, wherein the product stream comprises a molar ratio, H2:CO, of H2 to CO in the range of from 0.3:1 to 3.7:1 , more preferably in the range of from 0.4:1 to 3.6:1 , more preferably in the range of from 0.5:1 to 3.5:1 , more preferably in the range of from 0.6:1 to 3.4:1 , more preferably in the range of from 0.7:1 to 3.3:1 , more preferably in the range of from 0.8:1 to 3.2:1 , more preferably in the range of from 0.9:1 to 3.1 :1 , more preferably in the range of from 1 :1 to 3:1.

[0249] 94. The process of any one of embodiments 1 to 93, further comprising after (vi)

[0250] (vii) separating CO2from the product stream obtained in (vi), obtaining a stream comprising CO2 and a product stream being CO2 depleted.

[0251] 95. The process of embodiment 94, wherein separating CO2 is performed by a CO2 scrubber or by CO2 absorption.

[0252] 96. The process of embodiment 94 or 95, further comprising after (vii)

[0253] (viii) compressing the stream comprising CO2obtained from (vii), preferably to a stream having a pressure in the range of from 0.1 to 100 bara, preferably in the range of from 0.5 to 80 bara, more preferably in the range of from 0.8 to 60 bara, more preferably in the range of from 25 to 55 bara, more preferably in the range of from 45 to 55 bara.

[0254] 97. The process of any one of embodiments 1 to 96, further comprising after (vi), preferably after (vii), more preferably after (viii),

[0255] (ix) recycling at least a portion of the stream comprising CO2 obtained from (vii) or (viii) into the second feed stream prepared in (ii), more preferably recycling the stream comprising CO2obtained from (vii) or (viii) into the second feed stream prepared in (ii).

[0256] 98. The process of embodiment 97, wherein from 1 to 100 weight-%, preferably from 3 to 99 weight-%, more preferably from 5 to 98 weight-%, more preferably from 10 to 95 weight- %, more preferably from 15 to 90 weight-%, more preferably from 20 to 80 weight-%, more preferably from 25 to 75 weight-%, more preferably from 40 to 60 weight-%, of the second feed stream prepared in (ii) consist of the stream comprising CO2obtained from (vii) or (viii).

[0257] 99. The process of any one of embodiments 1 to 98, further comprising after (vi), preferably after (vii), more preferably after (viii),

[0258] (ix’) recycling at least a portion of the stream comprising CO2obtained from (vii) or (viii) into the second feed stream prepared in (ii), more preferably recycling the stream comprising CO2 obtained from (vii) or (viii) into the second feed stream prepared in (ii), wherein the weight ratio of CO2recycled to the second feed stream to the CO2comprised in the second feed stream prepared in (ii) is in the range of from 1 :1 to 5:1 , preferably in the range of from 1 :1 to 2:1 , more preferably in the range of from 1 :1 to 1.5:1.

[0259] 100. The process of embodiment 99, wherein from 1 to 100 weight-%, preferably from 25 to 75 weight-%, more preferably from 40 to 60 weight-%, of the CO2recycled to the second feed stream obtained from (ix’) consists of recycled CO2from the stream comprising CO2obtained in (vii) or (viii).

[0260] 101 . The process of any one of embodiments 1 to 100, further comprising after (vi), preferably after (viii), more preferably after (ix),

[0261] (x) adding H2 to the product stream obtained from (vi) or to the product stream being CO2 depleted obtained from (vii).

[0262] 102. The process of embodiment 101 , wherein H2 added to the product stream obtained from (vi) or to the product stream being CO2depleted obtained from (vii) comprises one or more of H2 obtained from a pipeline, H2 obtained from a tank, H2 obtained from a different process, preferably from a process for preparing styrene, and H2obtained from electrolysis, preferably from electrolysis using green power. 103. The process of any one of embodiments 1 to 102, wherein the molar ratio of CO2comprised in the product stream obtained in (vi) to CO2comprised in the reaction stream obtained in (v) is less than 1 :1.

[0263] 104. The process of any one of embodiments 1 to 103, wherein the product stream obtained from (vi) or the product stream being CO2depleted obtained from (vii) has a volume ratio, H2:CO2, of H2to CO in the range of from 0.9:1 to 2.9:1 , preferably in the range of from 1.3:1 to 2.5:1 , more preferably in the range of from 1.7:1 to 2.1 :1 , wherein the product stream obtained from (vi) or the product stream being CO2depleted obtained from (vii) more preferably has a volume ratio, H2:CO2, of H2to CO of 1.8:1.

[0264] 105. The process of any one of embodiments 1 to 104, comprising after (vi), preferably after (vii), more preferably after (viii), more preferably after (ix), more preferably after (x), the step:

[0265] (xi) converting the product stream comprising H2and CO obtainable by or obtained by the process according to any one of embodiments 1 to 104 or a chemical material obtainable by or obtained by the process according to any one of embodiments 1 to 104 to obtain a monomer, polymer or polymer product.

[0266] 106. The process of embodiment 105, wherein the monomer is a di- or polyol; preferably bu- tandiol; aldehyde; preferably formaldehyde; di- or polyisocyanate; preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (IPDI); amide; preferably caprolactam; alkene; preferably styrene, ethene and norbornene; alkyne, (di)ester; preferably methyl methacrylate; mono or diacid; preferably adipic acid or terephthalic acid; diamine; preferably hexamethylenediamine, nonanediamine; or sulfones; preferably 4,4'-dichlorodiphenyl sulfone.

[0267] 107. The process of embodiment 105 or 106, wherein the polymer is and / or the polymer product comprises polyamide (PA); preferably PA 6 or PA 66; polyisocyanate polyaddition product; preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or pol- yisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (PTFE), poly(me- thyl acrylate) (PM A), poly(methyl methacrylate) (PM MA), polybutadiene (BR, PBD), poly(cis-1 ,4-isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate co-tereph- thalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PHA), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymer or mixture thereof. The process of any one of embodiments 105 to 107, wherein the polymer and / or the polymer product is / are or is / are a part of: a part of a car; preferably cylinder head cover, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing, housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part, part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, cushion, or coating; a cloth; preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket; an electrical part; preferably electrical or electronic passive or active component, circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, microswitch, microbutton, semiconductor, reflector housing for light-emitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hook (snap-in), or spring tongue; a consumer, agricultural product or pharmaceutical product; preferably tennis string, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion, insulation, detergent, dishwasher tabs or powder, shampoo, body wash, shower gel, soap, fertilizer, fungicide, or pesticide; a packaging for the food industry; preferably mono- or multi-layer blown film, cast film (mono- or multi-layer), biaxially stretched film, or laminating film; or a part of a construction; preferably a rotor blade, insulating material, frame, housing, wall, coating, or separating wall. The process of any one of embodiments 105 to 108, wherein the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product 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 embodiment chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.

[0268] 110. The process of any one of embodiments 105 to 108, wherein the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product 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 embodiment chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard; wherein the feedstock comprises, preferably consists of, the sum of the afore-mentioned feed streams including the first feed stream comprising one or more organic compounds, the second feed stream comprising CO2 and optionally comprising O2 and the third feed stream comprising steam.

[0269] The unit bara refers to an absolute pressure of 105Pa.

[0270] The present invention is further illustrated by the following reference example, and examples.

[0271] EXAMPLES

[0272] Reference Example 1 : Determination of the viscosity of a liquid phase

[0273] Viscosity was measured at 20 °C according to the standard method DIN EN ISO 3219:1994 using a “Brookfield RV”-type laboratory viscosimeter employing spindles #4 or #5 at 100 revolutions per minute. Reference Example 2 and Example 3-5: Preparing a syngas

[0274] The process for preparing syngas was simulated with Aspen (version 14).

[0275] The conditions as noted in Table 1 below were set.

[0276] The prepared streams were mixed and reacted by gasification. Table 1

[0277] Conditions set for syngas preparation.

[0278] Table 2

[0279] Conditions set for syngas preparation.

[0280]

[0281] Table 3

[0282] Conditions set for syngas preparation.

[0283] As it can be gathered from the results, a novel process for preparing syngas can be provided wherein a plasma feed was used and wherein the amount of generated CO2 is reduced compared to a reference process. Further, no O2 has to be introduced as starting material in the pro- cess according to the present invention. Further, the process according to the present invention allows importing CO2 from other processes and also recycling of CO2 into the process as reactant. Further, the recycled CO2can be used for injecting a feed stream, optionally by spraying. In addition thereto, it has been found that by recycling CO2, a mass flow leveling can be achieved, resulting in a steady state process. CITED LITERATURE

[0284] - WO 2015 / 090575 A1

[0285] - WO 2021 / 180482 A1

[0286] - US 2016 / 0362355 A1 - US 2014 / 0239232 A1

[0287] - US 10435295 B2

[0288] - WO 2022 / 200532 A1

[0289] - KR 101882813 B1

[0290] - US 2022 / 234889 A1

Claims

Claims1 . Process for preparing syngas, the process comprising(i) preparing a first feed stream comprising one or more organic compounds;(ii) preparing a second feed stream comprising CO2 and optionally comprising O2;(iii) optionally preparing a third feed stream comprising steam;(iv) heating the second feed stream, or optionally combining and heating the first and second feed streams, or optionally combining and heating the second and third feed streams, or optionally combining and heating the first, second, and third feed streams, wherein the feed stream or the optionally combined feed streams are heated to a temperature in the range of from 1 ,000 to 20,000 °C;(v) combining the heated second feed stream obtained in (iv) with the first feed stream and optionally with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined first and second feed streams obtained in (iv) with the third feed stream, obtaining a reaction stream, or combining the heated and optionally combined second and third feed streams obtained in (iv) with the first feed stream, obtaining a reaction stream;(vi) feeding the heated and optionally combined first and second feed streams obtained in (iv), the heated and optionally combined first, second, and third feed streams obtained in (iv), or the reaction stream obtained in (v) in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2 and H2O, wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

2. The process of claim 1 , wherein in (iv) the feed stream or the combined feed stream is heated to a temperature in the range of from 1 ,000 to 20,000°C,.

3. Process for preparing syngas, the process comprising(i) preparing a first feed stream comprising one or more organic compounds;(ii) preparing a second feed stream comprising CO2 and optionally comprising O2;(iii) optionally preparing a third feed stream comprising steam;(iv) heating the second feed stream, or heating the optional third feed stream, or heating the second feed stream and the optional third feed stream, wherein the second feed stream, the optional third stream, or the second feed stream and the optional third feed stream are heated to a temperature in the range of from 1 ,000 to 20,000 °C;(v) combining the first feed stream, the second feed stream, and the optional third feed stream, obtaining a reaction stream;(vi) feeding the reaction stream in a reaction zone, obtaining a product stream comprising CO and H2, and optionally comprising CO2, H2O, or CO2 and H2O,wherein the one or more organic compounds independently from one another comprise C, H, and optionally one or more of O, S, and N.

4. The process of claim 3, wherein the second feed stream is heated in (iv) to a temperature in the range of from 1 ,000 to 20,000 °C.

5. The process of any one of claims 1 to 4, wherein from 49.5 to 100 weight-% of the one or more organic compounds consist of C.

6. The process of any one of claims 1 to 5, wherein the one or more organic compounds comprised in the first feed stream prepared in (i) are selected from the group consisting of CH4, C2H6, C3H8, C4H10, and mixtures of two or more thereof.

7. The process of any one of claims 1 to 6, wherein from 90 to 100 weight-% of the second feed stream prepared in (ii) consist of CO2.

8. The process of any one of claims 1 to 7, wherein heating in (iv) is directly or indirectly achieved by means of electricity.

9. The process of any one of claims 1 to 8, wherein heating in (iv) is achieved by one or more plasma generating means.

10. The process of any one of claims 1 to 9, wherein the maximum temperature of the reaction zone in (vi) is in the range of from 900 to 1 ,700 °C.11 . The process of any one of claims 1 to 10, wherein E(thermal) is thermal energy provided in (iv), (v), and (vi) for the reaction to syngas, wherein E(thermal) is the sum of the thermal energy provided by the combustion of the one or more organic compounds with oxygen gas in one or more of (iv), (v), and (vi) (E(combustion)) and the energy provided for heating in (iv) (E(heating)) according to formula I:E(thermal) = E(combustion) + E(heating) (I) wherein E(thermal) is comprised in the range of from 4 to 360 MJ per kg of the one or more organic compounds comprised in the first feed stream, wherein E(combustion) is comprised in the range of from 0 to 356 MJ per kg of the one or more organic compounds comprised in the first feed stream, and wherein E(heating) is comprised in the range of from 4 to 360 MJ per kg of the one or more organic compounds comprised in the first feed stream.

12. The process of claim 11 , wherein the amount of O2comprised in the second feed stream is varied, such that the amount of O2comprised in the second feed stream varies between0 and 10.5 kg per kg of the one or more organic compounds comprised in the first feed stream.

13. The process of any one of claims 1 to 12, further comprising after (vi)(vii) separating CO2 from the product stream obtained in (vi), obtaining a stream comprising CO2 and a product stream being CO2 depleted.

14. The process of any one of claims 1 to 13, further comprising after (vi),(ix) recycling at least a portion of the stream comprising CO2obtained from (vii) into the second feed stream prepared in (ii).

15. The process of any one of claims 1 to 14, wherein the molar ratio of CO2 comprised in the product stream obtained in (vi) to CO2 comprised in the reaction stream obtained in (v) is less than 1 :1.

16. The process of any one of claims 1 to 15, comprising after (vi) the step:(xi) converting the product stream comprising H2and CO obtainable by or obtained by the process according to any one of claims 1 to 15 or a chemical material obtainable by or obtained by the process according to any one of claims 1 to 15 to obtain a monomer, polymer or polymer product.

17. The process of claim 16, wherein the monomer is a di- or polyol, aldehyde, di- or polyisocyanate, polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (IPDI), amide, alkene, ethene and norbornene, alkyne, (di)ester, mono or diacid, , diamine, nonanediamine, or sulfones.

18. The process of claim 16 or 17, wherein the polymer is and / or the polymer product comprises polyamide (PA), polyisocyanate polyaddition product, thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR), low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (PTFE), poly(methyl acrylate) (PM A), poly(methyl methacrylate) (PM MA), polybutadiene (BR, PBD), poly(cis-1 ,4-isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate co-terephthalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PH A), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymer or mixture thereof.

19. The process of any one of claims 16 to 18, wherein the polymer and / or the polymer product is / are or is / are a part of: a part of a car, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing, housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part, part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, cushion, or coating; a cloth, trousers, pullover, boot, shoe, shoe sole, tight or jacket; an electrical part, circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, microswitch, microbutton, semiconductor, reflector housing for lightemitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hook (snap-in), or spring tongue; a consumer, agricultural product or pharmaceutical product, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion, insulation, detergent, dishwasher tabs or powder, shampoo, body wash, shower gel, soap, fertilizer, fungicide, or pesticide; a packaging for the food industry, cast film (mono- or multi-layer), biaxially stretched film, or laminating film; or a part of a construction, insulating material, frame, housing, wall, coating, or separating wall.

20. The process of any one of claims 16 to 19, wherein the content of the feedstock in the product stream comprising H2and CO, monomer, polymer or polymer product is 1 weight- % or more, and / or wherein the content of the feedstock in the product stream comprising H2 and CO, monomer, polymer or polymer product is 100 weight-% or less.

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