Process for preparing syngas from a liquid feedstock

Abstract

The present invention relates to a process for preparing syngas, the process comprising (i) preparing a first feed stream comprising a liquid phase and a gaseous phase, wherein the liquid phase comprises one or more organic compounds, and wherein the gaseous phase comprises CO2; (ii) preparing a second feed stream comprising O2 and optionally steam; (iii) mixing the first feed stream and the second feed stream; (iv) reacting the mixed feed stream obtained from (iii) in a reaction zone, obtaining a product stream comprising H2, CO, optionally CO2, and optionally H2O, wherein the one or more organic compounds comprise C, H, and optionally one or more of O, S, and N.

Description

[0001] Process for preparing syngas from a liquid feedstock

[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 at least a portion of the one or more organic compounds are provided in liquid form, and wherein the partial oxidation is preferably carried out without using a catalyst.

[0004] INTRODUCTION

[0005] Generally, syngas comprises H2 and CO, wherein one or both of CO2 and H2O can be comprised as well. Depending on the need, syngas can be prepared having a specific H2 to CO molar ratio. Preparation of syngas is typically done by partial oxidation of an organic compound in the presence of one or more of O2 and steam. CO2 can be generated as side-product and it can be separated from a product stream. Separated CO2 can also be recycled into the preparation process.

[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 hydrocarbons in the presence of oxygen and carbon dioxide, in which method at least a reactant gas containing hydrocarbons, 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 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 2016 / 0362355 A1 relates to preparation of an oil product of gasoline. The product contains hydrocarbon compound 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 down. Carbon dioxide (CO2) can be separated to be recycled back to the gasifier to be reused, archived or used otherwise for improves global environment. 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 rate, low nitrogen and sulfur pollution and a highly 'green' quality.

[0010] 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.

[0011] US 2022 / 234889 A1 relates to a method to control syngas composition by reactor temperature. In particular, a method of producing syngas is disclosed including partial oxidization of a hydro- carbonaceous feedstock material, wherein partial oxidation is carried out at specific reaction conditions.

[0012] EP 3878807 A1 relates to a process for the production of synthesis gas via allothermic gasification with controlled carbon dioxide reduction. In particular, a process for the production of synthesis gas by gasification of carbon-containing material is disclosed therein.

[0013] Since organic compounds exist in liquid form, there was a need for a process for preparing syngas using one or more organic compounds in liquid form.

[0014] It was therefore an object to provide a process for preparing syngas allowing processing of a liquid feedstock. Further, it was an object to provide a process for preparing syngas allowing recycling of CO2 for reducing needed amounts of O2 and steam. It was a further objective to provide a process for producing a syngas from a liquid, circular or liquid, non-circular feedstock, which particularly achieves a neutral CO2 balance. DETAILED DESCRIPTION

[0015] Thus, it has surprisingly been found that a feed stream comprising one or more organic compounds in a liquid phase can be used for preparing a syngas. Further, it has been found that CO2 which can be generated as side-product can be recycled into the process. By recycling of CO2 it was found that addition of O2 and H2O can be reduced. Further, it was found that recycled CO2 can be used for spraying the one or more organic compounds into the reaction zone. By that, a more efficient process can be provided, wherein in particular a higher yield of CO can be achieved.

[0016] Therefore, the present invention relates to a process for preparing syngas, the process comprising

[0017] (i) preparing a first feed stream comprising a liquid phase and a gaseous phase, wherein the liquid phase comprises one or more organic compounds, and wherein the gaseous phase comprises CO2;

[0018] (ii) preparing a second feed stream comprising O2 and optionally comprising steam;

[0019] (iii) mixing the first feed stream and the second feed stream, obtaining a mixed feed stream;

[0020] (iv) reacting the mixed feed stream obtained in (iii) in a reaction zone, obtaining a product stream comprising H2 and CO, 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.

[0021] 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 liquid phase comprised in the first feed stream prepared in (i) consist of C, H, and optionally one or more of O, S, and N.

[0022] It is preferred that from 49.5 to 100 weight-%, more preferably from 60 to 95 weight-%, more preferably form 70 to 95 weight-%, of the one or more organic compounds consist of C.

[0023] It is preferred that from 0.5 to 12 weight-%, more preferably from 2 to 11 weight-%, more preferably form 4 to 11 weight-%, of the one or more organic compounds consist of H.

[0024] It is preferred that from 0 to 50 weight-%, more preferably from 0 to 40 weight-%, more preferably from 0 to 30 weight-%, more preferably from 0 to equal to or smaller than 20 weight-%, of the one or more organic compounds consist of O.

[0025] It is preferred that from 0 to 10 weight-%, more preferably from 0 to 6 weight-%, more preferably from 0 to 4 weight-%, of the one or more organic compounds consist of S.

[0026] It is preferred that from 0 to 10 weight-%, more preferably from 0 to 6 weight-%, more preferably from 0 to 4 weight-%, of the one or more organic compounds consist of N. It is preferred that the one or more organic compounds comprised in the liquid phase 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, and mixtures thereof, wherein the one or more organic compounds preferably are pyrolysis oils.

[0027] In the case where the one or more organic compounds comprised in the liquid phase 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, 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.

[0028] Further in the case where the one or more organic compounds comprised in the liquid phase 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, and mixtures thereof, it is preferred that the heating oils are selected from the group consisting of (Ci-Cioo)hydrocarbons, preferably (C5-Cso)hy- drocarbons, more preferably (Cio-C6o)hydrocarbons, more preferably (Cn-C4o)hydrocarbons, more preferably (Ci2-C25)hydrocarbons, more preferably (Ci3-C2i)hydrocarbons, preferably (Cu- C2o)hydrocarbons.

[0029] 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.

[0030] It is preferred that the one or more organic compounds have a lower heating value in the range of from 20 to 60 MJ / kg, more preferably in the range of from 30 to 50 MJ / kg. 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 gaseous phase comprised in the first feed stream prepared in (i) consist of CO2.

[0031] It is preferred that the first feed stream prepared in (i) has a weight ratio, organic com- pounds:CC>2, of the one or more organic compounds to CO2 of equal to or greater than 1 :5, more preferably in the range of from 1 :5 to 1 ,000:1 , more preferably in the range of from 1 :5 to 500:1 , more preferably in the range of from 1 :5 to 100:1 , more preferably in the range of from 1 :5 to 50:1 , more preferably in the range of from 1 :1 to 25:1 , more preferably in the range of from 2:1 to 20:1 , more preferably in the range of from 5:1 to 15:1.

[0032] 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 first feed stream prepared in (i) consist of the one or more organic compounds and CO2.

[0033] It is preferred that the first feed stream prepared in (i) displays a multiphase flow regime, more preferably a two phase flow regime.

[0034] It is preferred according to a first alternative that the first feed stream prepared in (i) 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 first feed stream prepared in (i) preferably displays a horizontal flow.

[0035] It is preferred according to a second alternative that the first feed stream prepared in (i) displays a churn flow regime, an annular flow regime, a bubbly flow regime, a slag flow regime, or a mist flow regime, preferably an annular flow regime or a mist flow regime, more preferably a mist flow regime, wherein the first feed stream prepared in (i) preferably displays a vertical flow.

[0036] It is preferred that the liquid phase of the first feed stream prepared in (i) has a viscosity in the range of from 20 to 6,000 mPas, mor preferably in the range of from 100 to 5,000 mPas, wherein the viscosity is preferably determined according to Reference Example 1 .

[0037] It is preferred that the first feed stream prepared in (i) has a temperature in the range of from 50 to 220 °C, more preferably in the range of from 80 to 190 °C, more preferably in the range of from 110 to 160 °C.

[0038] 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 60 bara, more preferably in the range of from 42 to 52 bara.

[0039] 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 6,000 to 14,000 kg / h.

[0040] 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 O2.

[0041] It is preferred that the second feed stream prepared in (ii) comprises steam, wherein the second feed stream prepared in (ii) more preferably has a weight ratio, O2:steam, of O2, calculated as elemental O2, to steam, calculated as H2O, in the range of from 1 :10 to 100:1 , more preferably in the range of from 1 :1 to 61 :1.

[0042] It is preferred that the second feed stream prepared in (ii) has a temperature in the range of from 25 to 400 °C, more preferably in the range of from 50 to 300 °C, more preferably in the range of from 90 to 250 °C.

[0043] It is preferred that the second feed stream prepared in (ii) has a pressure in the range of from 5 to 80 bara, more preferably in the range of from 35 to 60 bara, more preferably in the range of from 40 to 52 bara.

[0044] It is preferred that the second feed stream prepared in (ii) 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 6,000 to 14,000 kg / h.

[0045] It is preferred that mixing in (iii) is conducted by spraying of the first feed stream and of the second feed stream, forming droplets and optionally liquid fragments of the liquid phase.

[0046] It is preferred that mixing in (iii) comprises

[0047] (111.1) mixing the first feed stream and the second feed stream, preferably in a mixing chamber, obtaining a mixed feed stream;

[0048] (111.2) feeding the mixed feed stream obtained in (iii.1) in a reaction zone.

[0049] In the case wherein mixing in (iii) comprises (iii.1) and (iii.2) as defined herein, it is preferred that mixing in (iii.1) is conducted by spraying of the mixed feed stream, forming droplets and optionally liquid fragments of the liquid phase.

[0050] Further in the case wherein mixing in (iii) comprises (iii.1) and (iii.2) as defined herein, it is preferred that feeding the mixed feed stream in the reaction zone is conducted by spraying of the mixed feed stream, forming droplets and optionally liquid fragments of the liquid phase. In the case wherein mixing in (iii.1 ) is conducted by spraying of the mixed feed stream, forming droplets and optionally liquid fragments of the liquid phase, it is preferred that spraying comprises applying a flow rate of the mixed feed stream in the range of from 100 to 1500 m3 / h, more preferably in the range of from 200 to 1000 m3 / h.

[0051] It is preferred that the mixed feed stream obtained in (iii) displays a multiphase flow regime, more preferably a two phase flow regime.

[0052] It is preferred that the mixed feed stream obtained in (iii) 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 mixed feed stream obtained in (iii) preferably displays a horizontal flow.

[0053] It is preferred that the mixed feed stream obtained in (iii) displays a churn flow regime, an annular flow regime, a bubbly flow regime, a slag flow regime, or a mist flow regime, preferably an annular flow regime or a mist flow regime, more preferably a mist flow regime, wherein the mixed feed stream obtained in (iii) preferably displays a vertical flow.

[0054] It is preferred that the mixed feed stream obtained in (iii) has a weight ratio, organic compounds^, of the one or more organic compounds to O2 in the range of from 0.10:1 to 2.00:1 , more preferably in the range of from 0.25:1 to 1.50:1.

[0055] It is preferred that the mixed feed stream obtained in (iii) has a weight ratio, CO2:O2, of CO2 to O2 in the range of from 1 :500 to 1 :10, more preferably in the range of from 1 :100 to 1 :5.0, more preferably in the range of from 1 :75 to 1 :2.0, more preferably in the range of from 1 :50 to 1 :1.5.

[0056] It is preferred that the mixed feed stream obtained in (iii) has a weight ratio, organic com- pounds:steam, of the one or more organic compounds to steam in the range of from 1 :1 to 100:1 , more preferably in the range of from 5:1 to 50:1 , more preferably in the range of from 7:1 to 41 :1 , more preferably in the range of from 20:1 to 25:1.

[0057] It is preferred that reacting in (iv) is conducted at a temperature in the range of from 1100 to 1500 °C, more preferably in the range of from 1200 to 1450 °C, more preferably in the range of from 1225 to 1425 °C.

[0058] It is preferred that reacting in (iv) is performed by gasification, more preferably entrained flow gasification (German “Flugstromvergasung”).

[0059] It is preferred that in (iv) the mixed feed stream displays a retention time in the reaction zone in the range of from 1 to 10 s. It is preferred that the product stream obtained in (iv) comprises a molar fraction of CO in the range of from 0.30 to 0.95, more preferably in the range of from 0.40 to 0.90, more preferably in the range of from 0.45 to 0.88.

[0060] It is preferred that the product stream obtained in (iv) comprises a molar fraction of H2 in the range of from 0.05 to 0.60, more preferably in the range of from 0.10 to 0.50, more preferably in the range of from 0.20 to 0.50.

[0061] It is preferred that the process further comprises after (iv)

[0062] (v) separating CO2 from the product stream obtained in (iv), obtaining a stream comprising CO2 and a product stream being CO2 depleted.

[0063] In the case wherein the process further comprises (v), it is preferred that separating CO2 is performed by a CO2 scrubber or by CO2 absorption.

[0064] Further in the case wherein the process further comprises (v), it is preferred that the process further comprises after (v)

[0065] (vi) compressing the stream comprising CO2 obtained in (v), preferably to a stream having a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0066] Further in the case wherein the process further comprises (v), preferably (v) and (vi), it is preferred according to a first alternative that the process further comprises after (v), preferably after

[0067] (vi)

[0068] (vii) recycling the stream comprising CO2 obtained in (v) or (vi) into the first feed stream prepared in (i).

[0069] In the case wherein the process further comprises (vii), 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 CO2 comprised in the first feed stream prepared in (i) consists of recycled CO2 from the stream comprising CO2 obtained in (v) or (vi).

[0070] Further in the case wherein the process further comprises (v), preferably (v) and (vi), it is preferred according to a second alternative that the process further comprises after (v), preferably after (vi)

[0071] (vii’) recycling the stream comprising CO2 obtained in (v) or (vi) into the first feed stream prepared in (i), wherein the weight ratio of CO2 recycled to the first feed stream to the CO2 comprised in the first feed stream prepared in (i) 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.

[0072] In the case wherein the process further comprises (vii’), 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 CO2 recycled to the first feed stream obtained from (vii’) consists of recycled CO2 from the stream comprising CO2 obtained in (v) or (vi).

[0073] It is preferred that the process further comprises after (iv), preferably after (v),

[0074] (viii) adding H2 to the product stream obtained in (iv) or to the product stream being CO2 depleted obtained in (v).

[0075] In the case wherein the process further comprises (viii), it is preferred that H2 added to the product stream obtained in (iv) or to the product stream being CO2 depleted obtained in (v) 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 H2 obtained from electrolysis, preferably from electrolysis using green power.

[0076] It is preferred that preparing the first feed stream in (i) comprises

[0077] (1.1 ) preparing a stream comprising one or more organic compounds;

[0078] (1.2) preparing a stream comprising CO2;

[0079] (1.3) mixing the stream comprising one or more organic compounds obtained in (i.1 ) and the stream comprising CO2 obtained in (i.2), obtaining the first feed stream.

[0080] In the case wherein preparing the first feed stream in (i) comprises (i.1 ), (i.2) and (i.3), it is preferred that the stream comprising one or more organic compounds prepared in (i.1 ) has a temperature in the range of from 10 to 350 °C, more preferably in the range of from 25 to 300 °C, more preferably in the range of from 50 to 200 °C, more preferably in the range of from 70 to 150 °C.

[0081] Further in the case wherein preparing the first feed stream in (i) comprises (i.1 ), (i.2) and (i.3), it is preferred that the stream comprising one or more organic compounds prepared in (i.1 ) has a pressure in the range of from 5 to 80 bara, more preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0082] Further in the case wherein preparing the first feed stream in (i) comprises (i.1 ), (i.2) and (i.3), it is preferred that the stream comprising one or more organic compounds prepared in (i.1 ) 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 6,000 to 14,000 kg / h.

[0083] Further in the case wherein preparing the first feed stream in (i) comprises (i.1 ), (i.2) and (i.3), it is preferred that the stream comprising CO2 prepared in (i.2) has a temperature in the range of from 25 to 380 °C, more preferably in the range of from 40 to 360 °C, more preferably in the range of from 60 to 300 °C.

[0084] Further in the case wherein preparing the first feed stream in (i) comprises (i.1), (i.2) and (i.3), it is preferred that the stream comprising CO2 prepared in (i.2) has a pressure in the range of from 5 to 80 bara, more preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0085] Further in the case wherein preparing the first feed stream in (i) comprises (i.1 ), (i.2) and (i.3), it is preferred that the stream comprising CO2 prepared in (i.2) 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 6,000 to 14,000 kg / h.

[0086] Further in the case wherein preparing the first feed stream in (i) comprises (i.1 ), (i.2) and (i.3), it is preferred that the stream comprising CO2 comprises one or more of CO2 recycled from (vii), CO2 recycled from (vii’), CO2 obtained from a different process for preparing syngas, CO2 obtained from a tank, CO2 obtained from a pipeline from another plant.

[0087] It is preferred that the second feed stream prepared in (ii) comprises steam, wherein preparing the second feed stream in (ii) comprises

[0088] (11.1 ) preparing a stream comprising O2;

[0089] (11.2) preparing a stream comprising steam;

[0090] (11.3) mixing the stream comprising O2 obtained in (ii.1 ) and the stream comprising steam obtained in (ii.2), obtaining the second feed stream.

[0091] In the case wherein the second feed stream prepared in (ii) comprises steam, and wherein preparing the second feed stream in (ii) comprises (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising O2 prepared in (ii.1 ) has a temperature in the range of from 25 to 400 °C, more preferably in the range of from 60 to 250 °C, more preferably in the range of from 120 to 190 °C.

[0092] Further in the case wherein the second feed stream prepared in (ii) comprises steam, and wherein preparing the second feed stream in (ii) comprises (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising O2 prepared in (ii.1 ) has a pressure in the range of from 5 to 80 bara, more preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0093] Further in the case wherein the second feed stream prepared in (ii) comprises steam, and wherein preparing the second feed stream in (ii) comprises (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising O2 prepared in (ii.1 ) 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 6,000 to 14,000 kg / h.

[0094] Further in the case wherein the second feed stream prepared in (ii) comprises steam, and wherein preparing the second feed stream in (ii) comprises (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising steam prepared in (ii.2) has a temperature in the range of from 200 to 500 °C, more preferably in the range of from 300 to 450 °C, more preferably in the range of from 350 to 425 °C.

[0095] Further in the case wherein the second feed stream prepared in (ii) comprises steam, and wherein preparing the second feed stream in (ii) comprises (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising steam prepared in (ii.2) has a pressure in the range of from 5 to 80 bara, more preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0096] Further in the case wherein the second feed stream prepared in (ii) comprises steam, and wherein preparing the second feed stream in (ii) comprises (ii.1 ), (ii.2) and (ii.3) as defined herein, it is preferred that the stream comprising steam prepared in (ii.2) has a mass flow rate smaller than 6,000 kg / h, more preferably smaller than 3,000 kg / h, more preferably smaller than 1 ,500 kg / h, more preferably smaller than 1 ,000 kg / h.

[0097] It is preferred that the molar ratio, CO2(product stream):CO2(mixed stream), of CO2 comprised in the product stream obtained in (iv) to CO2 comprised in the mixed stream obtained in (iii) is less than 1 :1.

[0098] It is preferred that the product stream obtained in (iv) or the product stream being CO2 depleted obtained in (v) has a volume ratio, H2:CO, of H2 to CO in the range of from 0.1 :1 to 1.5:1 , more preferably in the range of from 0.3:1 to 1.3:1 , more preferably in the range of from 0.4:1 to 1.1 :1.

[0099] The invention further relates to a method, preferably according to the method described herein, comprising the step:

[0100] - converting the product stream comprising H2 and 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.

[0101] 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.

[0102] 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.

[0103] In a preferred embodiment, the polymer and / or the polymer product is / are or is / are a part of:

[0104] - 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;

[0105] - a cloth, preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket;

[0106] - 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;

[0107] - 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;

[0108] - 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

[0109] - a part of a construction, preferably a rotor blade, insulating material, frame, housing, wall, coating, or separating wall. 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.

[0110] In a preferred embodiment, the content of C stemming from the product stream comprising H2 and CO which is contained in the monomer, polymer or polymer product is 1 weight-% or more, wherein C is calculated as the element, 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 C stemming from the product stream comprising H2 and CO which is contained in the monomer, polymer or polymer product is 100 weight-% or less, wherein C is calculated as the element, 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.

[0111] 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.

[0112] 1 . Process for preparing syngas, the process comprising (i) preparing a first feed stream comprising a liquid phase and a gaseous phase, wherein the liquid phase comprises one or more organic compounds, and wherein the gaseous phase comprises CO2;

[0113] (ii) preparing a second feed stream comprising O2 and optionally comprising steam;

[0114] (iii) mixing the first feed stream and the second feed stream, obtaining a mixed feed stream;

[0115] (iv) reacting the mixed feed stream obtained in (iii) in a reaction zone, obtaining a product stream comprising H2 and CO, 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.

[0116] 2. The process of embodiment 1 , 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 liquid phase comprised in the first feed stream prepared in (i) consist of C, H, and optionally one or more of O, S, and N.

[0117] 3. The process of embodiment 1 or 2, wherein from 49.5 to 100 weight-%, preferably from 60 to 95 weight-%, more preferably form 70 to 95 weight-%, of the one or more organic compounds consist of C.

[0118] 4. The process of any one of embodiments 1 to 3, wherein from 0.5 to 12 weight-%, preferably from 2 to 11 weight-%, more preferably from 4 to 11 weight-%, of the one or more organic compounds consist of H.

[0119] 5. The process of any one of embodiments 1 to 4, wherein from 0 to 50 weight-%, preferably from 0 to 40 weight-%, more preferably from 0 to 30 weight-%, more preferably from 0 to equal to or smaller than 20 weight-%, of the one or more organic compounds consist of O.

[0120] 6. The process of any one of embodiments 1 to 5, wherein from 0 to 10 weight-%, preferably from 0 to 6 weight-%, more preferably from 0 to 4 weight-%, of the one or more organic compounds consist of S.

[0121] 7. The process of any one of embodiments 1 to 6, wherein from 0 to 10 weight-%, preferably from 0 to 6 weight-%, more preferably from 0 to 4 weight-%, of the one or more organic compounds consist of N.

[0122] 8. The process of any one of embodiments 1 to 7, wherein the one or more organic compounds comprised in the liquid phase 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, and mixtures thereof, wherein the one or more organic compounds preferably are pyrolysis oils.

[0123] 9. The process of embodiment 8, 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.

[0124] 10. The process of embodiment 8 or 9, wherein the heating oils are selected from the group consisting of (Ci-Cioo)hydrocarbons, preferably (C5-C8o)hydrocarbons, more preferably (Cio-C6o)hydrocarbons, more preferably (Cn-C4o)hydrocarbons, more preferably (C12- C25)hydrocarbons, more preferably (Ci3-C2i)hydrocarbons, preferably (Ci4-C2o)hydrocar- bons.

[0125] 11 . The process of any one of embodiments 8 to 10, 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.

[0126] 12. The process of any one of embodiments 1 to 11 , wherein the one or more organic compounds have a lower heating value in the range of from 20 to 60 MJ / kg, preferably in the range of from 30 to 50 MJ / kg.

[0127] 13. The process of any one of embodiments 1 to 12, wherein from 90 to 100 weight-%, preferably from 95 to 100 weight-%, more preferably from 99 to 100 weight-%, of the gaseous phase comprised in the first feed stream prepared in (i) consist of CO2.

[0128] 14. The process of any one of embodiments 1 to 13, wherein the first feed stream prepared in (i) has a weight ratio, organic compounds:CC>2, of the one or more organic compounds to CO2 of equal to or greater than 1 :5, preferably in the range of from 1 :5 to 1 ,000:1 , more preferably in the range of from 1 :5 to 500:1 , more preferably in the range of from 1 :5 to

[0129] 100:1 , more preferably in the range of from 1 :5 to 50:1 , preferably in the range of from 1 :1 to 25:1 , more preferably in the range of from 2:1 to 20:1 , more preferably in the range of from 5:1 to 15:1.

[0130] 15. The process of any one of embodiments 1 to 14, wherein from 90 to 100 weight-%, preferably from 95 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 and CO2. 16. The process of any one of embodiments 1 to 15, wherein the first feed stream prepared in (i) displays a multiphase flow regime, preferably a two phase flow regime.

[0131] 17. The process of any one of embodiments 1 to 16, wherein the first feed stream prepared in (i) 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 first feed stream prepared in (i) preferably displays a horizontal flow.

[0132] 18. The process of any one of embodiments 1 to 16, wherein the first feed stream prepared in (i) displays a churn flow regime, an annular flow regime, a bubbly flow regime, a slag flow regime, or a mist flow regime, preferably an annular flow regime or a mist flow regime, more preferably a mist flow regime, wherein the first feed stream prepared in (i) preferably displays a vertical flow.

[0133] 19. The process of any one of embodiments 1 to 18, wherein the liquid phase of the first feed stream prepared in (i) has 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 .

[0134] 20. The process of any one of embodiments 1 to 19, wherein the first feed stream prepared in (i) has a temperature in the range of from 50 to 220 °C, preferably in the range of from 80 to 190 °C, more preferably in the range of from 110 to 160 °C.

[0135] 21 . The process of any one of embodiments 1 to 20, 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 60 bara, more preferably in the range of from 42 to 52 bara.

[0136] 22. The process of any one of embodiments 1 to 21 , 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 6,000 to 14,000 kg / h.

[0137] 23. The process of any one of embodiments 1 to 22, 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 O2.

[0138] 24. The process of any one of embodiments 1 to 23, wherein the second feed stream prepared in (ii) comprises steam, wherein the second feed stream prepared in (ii) preferably has a weight ratio, O2:steam, of O2, calculated as elemental O2, to steam, calculated as H2O, in the range of from 1 :10 to 100:1 , preferably in the range of from 1 :1 to 61 :1. 25. The process of any one of embodiments 1 to 24, wherein the second feed stream prepared in (ii) has a temperature in the range of from 25 to 400 °C, preferably in the range of from 50 to 300 °C, more preferably in the range of from 90 to 250 °C.

[0139] 26. The process of any one of embodiments 1 to 25, wherein the second feed stream prepared in (ii) has a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 40 to 52 bara.

[0140] 27. The process of any one of embodiments 1 to 26, wherein the second feed stream prepared in (ii) 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 6,000 to 14,000 kg / h.

[0141] 28. The process of any one of embodiments 1 to 27, wherein mixing in (iii) is conducted by spraying of the first feed stream and of the second feed stream, forming droplets and optionally liquid fragments of the liquid phase.

[0142] 29. The process of any one of embodiments 1 to 28, wherein mixing in (iii) comprises

[0143] (111.1) mixing the first feed stream and the second feed stream, preferably in a mixing chamber, obtaining a mixed feed stream;

[0144] (111.2) feeding the mixed feed stream obtained in (iii.1) in a reaction zone.

[0145] 30. The process of embodiment 29, wherein mixing in (iii.1 ) is conducted by spraying of the mixed feed stream, forming droplets and optionally liquid fragments of the liquid phase.

[0146] 31 . The process of embodiment 29 or 30, wherein feeding the mixed feed stream in the reaction zone is conducted by spraying of the mixed feed stream, forming droplets and optionally liquid fragments of the liquid phase.

[0147] 32. The process of embodiment 30 or 31 , wherein spraying comprises applying a flow rate of the mixed feed stream in the range of from 100 to 1500 m3 / h, preferably in the range of from 200 to 1000 m3 / h.

[0148] 33. The process of any one of embodiments 1 to 32, preferably of any one of embodiments 28 to 32, wherein the mixed feed stream obtained in (iii) displays a multiphase flow regime, preferably a two phase flow regime.

[0149] 34. The process of any one of embodiments 1 to 33, preferably of embodiment 33, wherein the mixed feed stream obtained in (iii) 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 mixed feed stream obtained in (iii) preferably displays a horizontal flow. 35. The process of any one of embodiments 1 to 33, preferably of embodiment 33, wherein the mixed feed stream obtained in (iii) displays a churn flow regime, an annular flow regime, a bubbly flow regime, a slag flow regime, or a mist flow regime, preferably an annular flow regime or a mist flow regime, more preferably a mist flow regime, wherein the mixed feed stream obtained in (iii) preferably displays a vertical flow.

[0150] 36. The process of any one of embodiments 1 to 35, wherein the mixed feed stream obtained in (iii) has a weight ratio, organic compounds:C>2, of the one or more organic compounds to O2 in the range of from 0.10:1 to 2.00:1 , preferably in the range of from 0.25:1 to 1.50:1.

[0151] 37. The process of any one of embodiments 1 to 36, wherein the mixed feed stream obtained in (iii) has a weight ratio, CO2:O2, of CO2 to O2 in the range of from 1 :500 to 1 :10, preferably in the range of from 1 :100 to 1 :5.0, more preferably in the range of from 1 :75 to 1 :2.0, more preferably in the range of from 1 :50 to 1 :1.5.

[0152] 38. The process of any one of embodiments 1 to 37, wherein the mixed feed stream obtained in (iii) has a weight ratio, organic compounds:steam, of the one or more organic compounds to steam in the range of from 1 :1 to 100:1 , preferably in the range of from 5:1 to 50:1 , more preferably in the range of from 7:1 to 41 :1 , more preferably in the range of from 20:1 to 25:1.

[0153] 39. The process of any one of embodiments 1 to 38, wherein reacting in (iv) is conducted at a temperature in the range of from 1100 to 1500 °C, preferably in the range of from 1200 to 1450 °C, more preferably in the range of from 1225 to 1425 °C.

[0154] 40. The process of any one of embodiments 1 to 39, wherein reacting in (iv) is performed by gasification, preferably entrained flow gasification (German “Flugstromvergasung”).

[0155] 41 . The process of any one of embodiments 1 to 40, wherein in (iv) the mixed feed stream displays a retention time in the reaction zone in the range of from 1 to 10 s.

[0156] 42. The process of any one of embodiments 1 to 41 , wherein the product stream obtained in (iv) comprises a molar fraction of CO in the range of from 0.30 to 0.95, preferably in the range of from 0.40 to 0.90, more preferably in the range of from 0.45 to 0.88.

[0157] 43. The process of any one of embodiments 1 to 42, wherein the product stream obtained in

[0158] (iv) comprises a molar fraction of H2 in the range of from 0.05 to 0.60, preferably in the range of from 0.10 to 0.50, more preferably in the range of from 0.20 to 0.50.

[0159] 44. The process of any one of embodiments 1 to 43, further comprising after (iv)

[0160] (v) separating CO2 from the product stream obtained in (iv), obtaining a stream comprising CO2 and a product stream being CO2 depleted. The process of embodiment 44, wherein separating CO2 is performed by a CO2 scrubber or by CO2 absorption. The process of embodiment 44 or 45, further comprising after (v)

[0161] (vi) compressing the stream comprising CO2 obtained in (v), preferably to a stream having a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara. The process of any one of embodiments 44 to 46, further comprising after (v), preferably after (vi)

[0162] (vii) recycling the stream comprising CO2 obtained in (v) or (vi) into the first feed stream prepared in (i). The process of embodiment 47, wherein from 1 to 100 weight-%, preferably from 25 to 75 weight-%, more preferably from 40 to 60 weight-%, of the CO2 comprised in the first feed stream prepared in (i) consists of recycled CO2 from the stream comprising CO2 obtained in (v) or (vi). The process of any one of embodiments 44 to 46, further comprising after (v), preferably after (vi)

[0163] (vii’) recycling the stream comprising CO2 obtained in (v) or (vi) into the first feed stream prepared in (i), wherein the weight ratio of CO2 recycled to the first feed stream to the CO2 comprised in the first feed stream prepared in (i) 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. The process of embodiment 49, wherein from 1 to 100 weight-%, preferably from 25 to 75 weight-%, more preferably from 40 to 60 weight-%, of the CO2 recycled to the first feed stream obtained from (vii’) consists of recycled CO2 from the stream comprising CO2 obtained in (v) or (vi). The process of any one of embodiments 1 to 50, further comprising after (iv), preferably after (v),

[0164] (viii) adding H2 to the product stream obtained in (iv) or to the product stream being CO2 depleted obtained in (v). The process of embodiment 51 , wherein H2 added to the product stream obtained in (iv) or to the product stream being CO2 depleted obtained in (v) 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 H2 obtained from electrolysis, preferably from electrolysis using green power. The process of any one of embodiments 1 to 52, wherein preparing the first feed stream in (i) comprises

[0165] (1.1) preparing a stream comprising one or more organic compounds;

[0166] (1.2) preparing a stream comprising CO2;

[0167] (1.3) mixing the stream comprising one or more organic compounds obtained in (i.1) and the stream comprising CO2 obtained in (i.2), obtaining the first feed stream. The process of embodiment 53, wherein the stream comprising one or more organic compounds prepared in (i.1) has a temperature in the range of from 10 to 350 °C, preferably in the range of from 25 to 300 °C, more preferably in the range of from 50 to 200 °C, more preferably in the range of from 70 to 150 °C. The process of embodiment 53 or 54, wherein the stream comprising one or more organic compounds prepared in (i.1) has a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara. The process of any one of embodiments 53 to 55, wherein the stream comprising one or more organic compounds prepared in (i.1) 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 6,000 to 14,000 kg / h. The process of any one of embodiments 53 to 56, wherein the stream comprising CO2 prepared in (i.2) has a temperature in the range of from 25 to 380 °C, preferably in the range of from 40 to 360 °C, more preferably in the range of from 60 to 300 °C. The process of any one of embodiments 53 to 57, wherein the stream comprising CO2 prepared in (i.2) has a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara. The process of any one of embodiments 53 to 58, wherein the stream comprising CO2 prepared in (i.2) 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 6,000 to 14,000 kg / h. The process of any one of embodiments 53 to 59, wherein the stream comprising CO2 comprises one or more of CO2 recycled from (vii), CO2 recycled from (vii’), CO2 obtained from a different process for preparing syngas, CO2 obtained from a tank, CO2 obtained from a pipeline from another plant. The process of any one of embodiments 1 to 60, wherein the second feed stream prepared in (ii) comprises steam, wherein preparing the second feed stream in (ii) comprises (ii.1) preparing a stream comprising O2; (11.2) preparing a stream comprising steam;

[0168] (11.3) mixing the stream comprising O2 obtained in (ii.1) and the stream comprising steam obtained in (ii.2), obtaining the second feed stream.

[0169] 62. The process of embodiment 61 , wherein the stream comprising O2 prepared in (ii.1) has a temperature in the range of from 25 to 400 °C, preferably in the range of from 60 to 2500C, more preferably in the range of from 120 to 190 °C.

[0170] 63. The process of embodiment 61 or 62, wherein the stream comprising O2 prepared in (ii.1) has a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0171] 64. The process of any one of embodiments 61 to 63, wherein the stream comprising O2 prepared in (ii.1) 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 6,000 to 14,000 kg / h.

[0172] 65. The process of any one of embodiments 61 to 64, wherein the stream comprising steam prepared in (ii.2) has a temperature in the range of from 200 to 500 °C, preferably in the range of from 300 to 450 °C, more preferably in the range of from 350 to 425 °C.

[0173] 66. The process of any one of embodiments 61 to 65, wherein the stream comprising steam prepared in (ii.2) has a pressure in the range of from 5 to 80 bara, preferably in the range of from 35 to 60 bara, more preferably in the range of from 42 to 52 bara.

[0174] 67. The process of any one of embodiments 61 to 66, wherein the stream comprising steam prepared in (ii.2) has a mass flow rate smaller than 6,000 kg / h, preferably smaller than 3,000 kg / h, more preferably smaller than 1 ,500 kg / h, more preferably smaller than 1 ,000 kg / h.

[0175] 68. The process of any one of embodiments 1 to 67, wherein the molar ratio, CO2(product stream):CO2(mixed stream), of CO2 comprised in the product stream obtained in (iv) to CO2 comprised in the mixed stream obtained in (iii) is less than 1 :1.

[0176] 69. The process of any one of embodiments 1 to 68, wherein the product stream obtained in (iv) or the product stream being CO2 depleted obtained in (v) has a volume ratio, H2:CO, of H2 to CO in the range of from 0.1 :1 to 1.5:1 , preferably in the range of from 0.3:1 to 1.3:1 , more preferably in the range of from 0.4:1 to 1.1 :1.

[0177] 70. The process of any one of embodiments 1 to 69, comprising after (iv), preferably after (v), more preferably after (vi), more preferably after (vii), more preferably after (viii), the step: (ix) converting the product stream comprising H2 and CO obtainable by or obtained by the process according to any one of embodiments 1 to 69, or a chemical material obtainable by or obtained by the process according to any one of embodiments 1 to 69, to obtain a monomer, polymer, or polymer product.

[0178] 71 . The process of embodiment 70, 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.

[0179] 72. The process of embodiment 70 or 71 , 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 polyiso- cyanurate (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 (PHA), poly-3-hydroxy- butyrate (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.

[0180] 73. The process of any one of embodiments 70 to 72, 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 70 to 73, 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. The process of any one of embodiments 70 to 73, wherein the content of C stemming from the product stream comprising H2 and CO which is contained in the monomer, polymer or polymer product is 1 weight-% or more, wherein C is calculated as the element, 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 C stemming from the product stream comprising H2 and CO which is contained in the monomer, polymer or polymer product is 100 weight-% or less, wherein C is calculated as the element, 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.

[0181] The unit bara refers to an absolute pressure of 105Pa.

[0182] The present invention is further illustrated by the following examples.

[0183] EXAMPLES

[0184] Reference Example 1 : Determination of the viscosity of a liquid phase

[0185] 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.

[0186] Comparative Example 0 and Examples 1-5: Process for preparing syngas

[0187] A process for preparing syngas was simulated with Aspen (Aspen version V14). For preparing a first feed stream according to the present invention a feed stream comprising organic compounds was mixed with a CO2 containing feed stream.

[0188] The conditions as noted in Tables 1-3 below were set. The pressure for high vacuum residue stream, CO2 stream, steam stream for the first feed stream, O2 stream, steam stream for the second feed stream, first feed stream, and second feed stream was set independently from each other to 47 bara.

[0189] The prepared streams were mixed and reacted by gasification.

[0190] Table 1 .

[0191] Settings for Comparative Example 0, and Examples 1-5. Table 2.

[0192] Settings for Comparative Example 6, and Examples 7-11 . Table 3.

[0193] Settings for Examples 12-14. Table 4.

[0194] Settings for Examples 15-16 and Comparative Example 17.

[0195] In Examples 15 and 16, the weight ratio of organics to CO2 in the first feed stream was 47 and 0.22, respectively.

[0196] In Comparative Example 17, the weight ratio of organics to CO2 in the first feed stream was 0.18. Due to the CO2 the flame is unable to develop, such that no gasification reaction occurred. Thus, the simulation could not run since the necessary temperature in the reactor was not reached. Therefore, no results were obtained for Comparative Example 17. As it can be gathered from the results, a process for preparing syngas can be provided wherein the amount of steam can be reduced. Further, the process according to the present invention allows recycling of CO2. In particular, the recycled CO2 can be used for spraying a liquid feed stream. Thus, a syngas can be prepared according to the present invention having a comparatively high CO content. 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

[0197] - WO 2015 / 090575 A1

[0198] - WO 2022 / 200532 A1

[0199] - US 10435295

[0200] - US 2016 / 0362355 A1 - WO 2021 / 180482 A1

[0201] - US 2022 / 234889 A1

[0202] - EP 3878807 A1

Claims

Claims1 . Process for preparing syngas, the process comprising(i) preparing a first feed stream comprising a liquid phase and a gaseous phase, wherein the liquid phase comprises one or more organic compounds, and wherein the gaseous phase comprises CO2, wherein the first feed stream prepared in (i) has a weight ratio, organic compounds:CC>2, of the one or more organic compounds to CO2 of equal to or greater than 1 :5;(ii) preparing a second feed stream comprising O2 and optionally comprising steam;(iii) mixing the first feed stream and the second feed stream, obtaining a mixed feed stream;(iv) reacting the mixed feed stream obtained in (iii) in a reaction zone, obtaining a product stream comprising H2 and CO, 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 the one or more organic compounds comprised in the liquid phase are selected from the group consisting of pyrolysis oils, heating oils, vacuum residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, bio oils, fuel oils, pyrolysis gasolines, tire pyrolysis oils (TPO), waste oils, used oils, and mixtures thereof.

3. The process of claim 1 or 2, wherein the first feed stream prepared in (i) has a weight ratio, organic compounds:CC>2, of the one or more organic compounds to CO2 in the range of from 1 :5 to 1 ,000:1.

4. The process of any one of claims 1 to 3, wherein the first feed stream prepared in (i) has a temperature in the range of from 50 to 220 °C.

5. The process of any one of claims 1 to 4, wherein the first feed stream prepared in (i) has a pressure in the range of from 5 to 80 bara.

6. The process of any one of claims 1 to 5, wherein the second feed stream prepared in (ii) has a temperature in the range of from 25 to 400 °C.

7. The process of any one of claims 1 to 6, wherein the second feed stream prepared in (ii) has a pressure in the range of from 5 to 80 bara.

8. The process of any one of claims 1 to 7, wherein mixing in (iii) is conducted by spraying of the first feed stream and of the second feed stream, forming droplets and optionally liquid fragments of the liquid phase.

9. The process of any one of claims 1 to 8, wherein the mixed feed stream obtained in (iii) has a weight ratio, organic compounds:C>2, of the one or more organic compounds to O2 in the range of from 0.10:1 to 2.00:1.

10. The process of any one of claims 1 to 9, wherein the mixed feed stream obtained in (iii) has a weight ratio, CO2:O2, of CO2 to O2 in the range of from 1 :500 to 1 :10.11 . The process of any one of claims 1 to 10, wherein reacting in (iv) is conducted at a temperature in the range of from 1100 to 1500 °C.

12. The process of any one of claims 1 to 11 , wherein reacting in (iv) is performed by gasification.

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

14. The process of claim 13, further comprising after (v)(vi) compressing the stream comprising CO2 obtained in (v).

15. The process of claim 13 or 14, further comprising after (v)(vii) recycling the stream comprising CO2 obtained in (v) or (vi) into the first feed stream prepared in (i).

16. The process of any one of claims 1 to 15, comprising after (iv) the step:(ix) converting the product stream comprising H2 and 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), polystyrene 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 C stemming from the product stream comprising H2 and CO which is contained in the monomer, polymer or polymer product is 1 weight-% or more, and / or wherein the content of C stemming from the product stream comprising H2 and CO which is contained in the monomer, polymer or polymer product is 100 weight-% or less.

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