Carbon black from particulate raw material

Abstract

The present invention relates to a process for the production of carbon black in an entrained flow reactor by using particulate carbon-containing feedstock.

Description

1 / 106 Carbon black from particulate raw material TECHNICAL FIELD

[001] The present invention relates to a process for the production of carbon black in an entrained flow reactor using feedstock containing particulate carbon. TECHNICAL BACKGROUND

[002] Carbon black production involves the cracking or thermal decomposition of a carbon-containing feedstock in a reaction chamber at temperatures such as 800°C (e.g., in the temperature range of 1100°C to 2000°C). These high temperatures are obtained by combustion of a mixture consisting of oxygen-containing gas and a combustion fuel (i.e., fuel). The carbon black (CB) carried by the gases (hot gas stream) exiting the reaction chamber is then cooled in a quenching operation and subsequently collected by any suitable means conventionally employed in the art.

[003] Carbon black has numerous applications, such as reinforcing or filling agents for the rubber and tire industries. In addition, carbon black has seen increasing use in other areas, such as dyes and reprographic toners for photocopiers. The diverse applications of carbon black require a diverse range of characteristics, such as particle size, structure, yield, surface area, and coloration.

[004] Carbon black formation can be separated into different stages of the process, including raising the temperature of the raw material to the pyrolysis temperature, pyrolysis of the raw material to unsaturated species such as acetylene and aromatic-containing intermediate products, nuclei formation, surface growth and aggregation. Petition 870250076402, dated 08 / 28 / 2025, page 9 / 136 2 / 106

[005] In the prior art, the feedstock for the production of carbon black in an entrained flow reactor, such as in a furnace reactor, was limited to feedstocks containing liquid carbon. Feedstocks containing liquid carbon are, for example, liquid hydrocarbons, such as cracking oils, such as oils derived from steam cracking or fluidized catalytic cracking.

[006] Immediately after injecting liquid carbon-containing feedstocks into a carbon black reactor, the feedstock evaporates and carbon black is formed. The transformation of particulate carbon-containing feedstocks into gaseous components is considerably slower compared to liquid carbon-containing feedstocks, making it difficult to obtain a desirable pyrolysis of particulate carbon-containing feedstocks.

[007] As an alternative approach, feedstock containing particulate carbon, such as tires, can be pyrolyzed in a pyrolysis reactor. Pyrolysis is carried out at low temperatures, such as 500°C, and liquid, gaseous and solid fractions are obtained. The liquid fraction can then be used to produce new or virgin carbon black (nCB) in an entrained flow reactor, such as a furnace reactor.

[008] US patent 2002 / 0117388 A1 refers to the pyrolysis of discarded rubber materials, including used tires, mentioned previously. The objective of US patent 2002 / 0117388 A1 is to recover components present in discarded rubber materials, such as carbon black. After pyrolysis, carbon black can be recovered from the pyrolysis gas (recovered carbon black rCB).

[009] However, the solid yield of pyrolysis at low temperatures is low, requiring a subsequent manufacturing process to obtain carbon black from the liquid fraction of pyrolysis. In addition, the coke content and ash content of the carbon black Petition 870250076402, dated 08 / 28 / 2025, page 10 / 136 3 / 106 recovered after pyrolysis are undesirable.

[0010] Consequently, a method must be developed for the manufacture of carbon black that allows the use of feedstocks containing particulate carbon. Surprisingly, it has been found that feedstock containing particulate carbon can be used in an entrained flow reactor, in which the hot gas stream has a temperature of at least 800°C. SUMMARY OF THE INVENTION

[0011] The objective is achieved by a method for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, comprising: (a) providing a hot gas stream, (b) providing a feedstock containing particulate carbon and (d) injecting the feedstock containing particulate carbon into the hot gas stream to form carbon black, wherein the hot gas stream has a temperature of at least 800°C.

[0012] In addition, carbon black produced according to the inventive method is provided, as well as a composition comprising (A) an elastomeric polymeric material and (B) carbon black obtained according to the invention and an article made of or comprising the inventive composition.

[0013] In addition, carbon black is provided, wherein (I) carbon black has a BET surface area of ​​80 to 90 m2 / g, preferably a BET surface area of ​​85 to 88 m2 / g, and a compressed oil absorption number of 58 to 69 mL / 100 g, preferably a compressed oil absorption number of 61 to 64 mL / 100 g, preferably an STSA surface area of ​​72 to 82 m2 / g, more preferably an STSA surface area of ​​76 to 79 m2 / g, preferably volatiles of 2.1 to 2.7% by weight, more preferably volatiles of 2.3 to 2.5% by weight, preferably a transmittance Petition 870250076402, dated 08 / 28 / 2025, page 11 / 136 4 / 106 cia at 425 nm in toluene greater than 50%, more preferably a transmittance at 425 nm in toluene greater than 77%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D6556-21, wherein the volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 161818 against toluene; and / or (II) carbon black with a BET surface area of ​​70 to 85 m2 / g, preferably a BET surface area of ​​77 to 79 m2 / g, and a compressed oil absorption number of 59 to 70 mL / 100 g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​68 to 78 m2 / g, more preferably an STSA surface area of ​​71 to 73 m2 / g,preferably a compressed oil absorption number of 58 to 69 mL / 100 g, more preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably volatiles of 2.0 to 2.6% by weight, more preferably volatiles of 2.2 to 2.4% by weight, preferably a transmittance at 425 nm in toluene greater than 40%, more preferably a transmittance at 425 nm in toluene greater than 56%, wherein the BET surface area is measured in accordance with ASTM D655621, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D6556-21, wherein the volatiles are measured at 950°C for 7 minutes, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 relative to toluene; and / or (III) carbon black with a BET surface area of ​​80 to 96 m2 / g, preferably a BET surface area of ​​89 to 92 m2 / g,and a number of absorbers, Petition 870250076402, dated 08 / 28 / 2025, page 12 / 136 5 / 106 compressed oil absorption of 60 to 69 mL / 100 g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably a STSA surface area of ​​79 to 87 m² / g, more preferably a STSA surface area of ​​82 to 84 m² / g, preferably volatiles of 2.2 to 2.9% by weight, more preferably volatiles of 2.5 to 2.7% by weight, preferably a transmittance at 425 nm in toluene greater than 40%, more preferably a transmittance at 425 nm in toluene greater than 62%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D6556-21, where volatiles are measured at 950°C for 7 min, as described in the descriptive report,and the transmittance at 425 nm in toluene is measured according to ASTM D 161818 against toluene; and / or (IV) carbon black with a BET surface area of ​​120 to 138 m² / g, preferably a BET surface area of ​​127 to 130 m² / g, and a compressed oil absorption number of 58 to 69 mL / 100 g, preferably a compressed oil absorption number of 62 to 64 mL / 100 g, preferably an STSA surface area of ​​82 to 95 m² / g, more preferably an STSA surface area of ​​87 to 89 m² / g, preferably volatiles of 2.6 to 3.2% by weight, more preferably volatiles of 2.8 to 3.0% by weight, preferably a transmittance at 425 nm in toluene greater than 60%, more preferably a transmittance at 425 nm in toluene greater than 80%, wherein the BET surface area is measured in accordance with ASTM. D6556-21, the compressed oil absorption number is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21,where volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene, Petition 870250076402, dated 08 / 28 / 2025, page 13 / 136 6 / 106 is measured according to ASTM D 1618-18 against toluene; and / or (V) carbon black with a BET surface area of ​​82 to 95 m² / g, preferably a BET surface area of ​​86 to 89 m² / g, and a compressed oil absorption number of 59 to 70 mL / 100 g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​70 to 82 m² / g, more preferably an STSA surface area of ​​76 to 78 m² / g, preferably volatiles of 1.8 to 2.4% by weight, more preferably volatiles of 2.0 to 2.2% by weight, preferably a transmittance at 425 nm in toluene greater than 60%, more preferably a transmittance at 425 nm in toluene greater than 80%, wherein the BET surface area is measured in accordance with ASTM. D655621, the compressed oil absorption number is measured according to ASTM D3493-20 using paraffinic oil, the STSA surface area is measured according to ASTM D6556-21,where volatiles are measured at 950°C for 7 min, as described in the descriptive report, and transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 against toluene.

[0014] In addition, the raw material containing particulate carbon is used for the manufacture of carbon black in an entrained flow reactor.

[0015] Furthermore, a method is provided for adjusting the position of the cooler in an entrained flow reactor for the production of carbon black from a feedstock containing particulate carbon, comprising: I) injecting a feedstock containing particulate carbon into a hot gas stream of an entrained flow reactor, wherein the hot gas stream has a temperature of at least 800°C; II) cooling the hot gas stream comprising the carbon black produced; III) measuring the transmittance of the carbon black produced; IV) adjusting the position of the cooler in the entrained flow reactor. Petition 870250076402, dated 08 / 28 / 2025, page 14 / 136 7 / 106 until the transmittance of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene. BRIEF DESCRIPTION OF THE DRAWINGS

[0016] Figure 1: Section of a furnace reactor

[0017] Figure 2: Feeding and mixing device consisting of a nozzle

[0018] Figure 3: Lapel nozzle for feeding and mixing device

[0019] Figure 4: Deagglomeration conduit for the feeding and mixing device

[0020] Figure 5: Feeding and mixing device without nozzle DETAILED DESCRIPTION

[0021] It should be noted that, as used in the descriptive report and appended claims, the singular forms a, an, aeo include plural referents unless the context clearly indicates otherwise. Thus, for example, reference to an oxygen-containing gas includes mixtures of oxygen-containing gases, reference to a fuel includes mixtures of two or more such fuels, and the like.

[0022] Diameter always refers to the internal diameter of an object, unless otherwise indicated. For example, the diameter of a tubular conduit refers to the internal diameter of the tubular conduit.

[0023] The term raw material refers to the raw material for the production of carbon black. According to the present invention, a particulate raw material is used for the production of carbon black. The term or abbreviation raw material used in the present invention Petition 870250076402, dated 08 / 28 / 2025, p. 15 / 136 8 / 106 vulgação refers to raw material containing particulate carbon.

[0024] The term hot gas stream refers to a carrier gas in an entrained flow reactor, such as a furnace reactor, which brings the reaction mixture (comprising the feedstock containing carbon particles) to the temperature required for the pyrolysis reaction. For example, the hot gas stream is the gas stream after combustion of the fuel in a furnace reactor.

[0025] Carbon black, as referred to herein, means a material composed substantially, for example, of more than 80% by weight, or more than 90% by weight, or more than 95% by weight, based on its total weight, of carbon, produced by pyrolysis or radical abstraction of non-carbonaceous atoms from a carbon-containing feedstock. Different industrial processes are known for the production of carbon blacks, such as the furnace process, the gas black process, the acetylene black process, the thermal carbon black process, or the lamp carbon black process. The production of carbon blacks is, in itself, well known in the art and, for example, described in J.-B. Donnet et al., Carbon Black: Science and Technology, 2nd edition, and is therefore not described here in more detail.

[0026] The reaction volume of the reactor is the volume of the reactor between the injection position of the feedstock containing particulate carbon and the cooling position.

[0027] The present invention relates to a method for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, comprising: (a) supplying a hot gas stream, (b) supplying a feedstock containing particulate carbon and (d) injecting the feedstock containing particulate carbon into the hot gas stream to form carbon black, Petition 870250076402, dated 08 / 28 / 2025, p. 16 / 136 9 / 106 where the hot gas flow has a temperature of at least 800°C.

[0028] Without limiting oneself to theory, it is believed that the heating rate of particulate carbon-containing feedstock is lower compared to that of liquid carbon-containing feedstock, so it is desirable that particulate carbon-containing feedstock be injected into the hot gas stream of an entrained flow reactor at a suitable temperature of 800°C or even higher. For example, the hot gas stream temperature may be at least 900°C, at least 1000°C, at least 1100°C, at least 1200°C, at least 1300°C, at least 1400°C, at least 1500°C, and at least 1600°C. The desired minimum temperature can be determined by measuring the transmittance of the carbon black produced. If the transmittance is low, the hot gas stream temperature can be increased.

[0029] Hot gas flow can be obtained by electrical preheating, plasma heating, and combustion of a fuel gas containing oxygen. Hot gas flow can be provided by (a1) supplying fuel and oxygen-containing gas to a reactor combustion chamber, (b2) combustion of the fuel in the combustion chamber to produce hot gas flow.

[0030] Consequently, the present invention may relate to a method for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, comprising: (a) supplying fuel and oxygen-containing gas to a combustion chamber of the reactor, (b) burning fuel in the combustion chamber to produce hot combustion gases, (d) injecting the feedstock containing particulate carbon into the hot gas stream to form carbon black, wherein the gases of Petition 870250076402, dated 08 / 28 / 2025, page 17 / 136 10 / 106 hot combustion elements have a temperature of at least 800°C.

[0031] The feedstock containing particulate carbon may comprise inert compounds, coke, compounds containing C,H and / or carbon black, preferably carbon black and compounds containing C,H. The feedstock containing particulate carbon consists of particles and, generally, agglomerated particles. In contrast, a liquid feedstock containing carbon means that the feedstock is liquid at 20°C and 1 atm. It is preferable that the carbon black production method does not use liquid feedstock containing carbon for the production of carbon black.

[0032] Generally, all raw materials for the production of carbon black are raw materials containing particulate carbon.

[0033] The aforementioned particulate raw material may contain up to 10% by weight of an oil (extender oil). For example, rubber granules often contain up to 10% by weight of an oil (extender oil). The said oil or extender oil is generally an aliphatic or aromatic oil.

[0034] Raw material containing carbon particles is a suitable raw material for producing carbon black, i.e., new carbon black. Therefore, raw material containing carbon particles comprises materials that can be pyrolyzed.

[0035] The C,H-containing compound (hydrocarbon compound) can be used to produce carbon black, namely new carbon black (nCB) or virgin carbon black (vCB). C,H-containing compounds refer to compounds that each comprise C and H. For example, C,H-containing compounds are hydrocarbon compounds that may comprise heteroatoms such as O or S.

[0036] The raw material containing particulate carbon may comprise from 10 to 100% by weight of compounds containing C,H, preferably from 20 to 99% by weight of compounds containing C,H, more Petition 870250076402, dated 08 / 28 / 2025, page 18 / 136 11 / 106 preferably 30 to 90% by weight of compounds containing C,H and, more preferably, 40 to 70% by weight of compounds containing C,H, based on the total weight of the raw material containing particulate carbon.

[0037] Raw materials containing particulate carbon may comprise inert compounds, and inert compounds may comprise metals, metallic compounds, silicon and silica. Metals may be zinc, silicon, calcium, aluminum and / or iron.

[0038] The particulate carbon-containing raw material may comprise from 1 to 40% by weight of inert compounds, preferably from 3 to 30% by weight of inert compounds, more preferably from 4 to 20% by weight of inert compounds and, most preferably, from 5 to 15% by weight of inert compounds, based on the total weight of the particulate carbon-containing raw material.

[0039] The particulate carbon-containing feedstock may additionally contain carbon black, i.e., recovered carbon black. This carbon black is typically present in tires and can therefore be recovered. The particulate carbon-containing feedstock must contain 1 to 70% by weight of carbon black, preferably 5 to 60% by weight of carbon black, more preferably 10 to 50% by weight of carbon black, and even more preferably 15 to 40% by weight of carbon black, based on the total weight of the particulate carbon-containing feedstock. Alternatively, the particulate carbon-containing feedstock is free of recovered carbon black.

[0040] In this context, recovered carbon black means carbon black that can be recovered in the process. In other words, carbon black present in the raw material and not produced in the inventive process.

[0041] Compounds containing C,H are, for example, rubber, Petition 870250076402, dated 08 / 28 / 2025, page 19 / 136 12 / 106 plastic and / or biomass-based materials. The particulate carbon-containing feedstock is preferably supplied as granules (i.e., carbon-containing granulated feedstock). Consequently, the particulate carbon-containing feedstock may comprise or be rubber granules, plastic granules, and / or biomass-based granules. Consequently, the particulate carbon-containing feedstock may be particulate rubber feedstock, particulate plastic feedstock, and / or particulate biomass-based feedstock. It is preferable that the particulate carbon-containing feedstock comprises rubber granules, wherein the rubber granules comprise carbon black.

[0042] A biomass-based feedstock can be distinguished from a fossil-based feedstock by measuring the C14 content (C14 content) in the feedstock (radiocarbon dating). The relative amount of C14 atoms compared to C12 (C14 / C12 / C12 ratio) is lower in a fossil-based feedstock compared to a biomass-based feedstock. Consequently, a fossil-based feedstock is one that has a relative amount of C14 atoms compared to C12 that is lower than the relative amount of naturally occurring (or biologically derived) C14 atoms compared to C12.

[0043] Preferably, the amount of particulate biomass-based feedstock in particulate carbon-containing feedstock is 20 to 100% by weight, such as 40 to 100% by weight, 50 to 99% by weight, 60 to 95% by weight, or 60 to 80% by weight based on the total weight of the particulate carbon-containing feedstock.

[0044] Preferably, the amount of particulate rubber granules in the carbon-containing raw material is 20 to 100% by weight, such as 40 to 100% by weight, 50 to 99% by weight, 60 to 95% by weight, or 80 to 90% by weight, based on the total weight of the raw material. Petition 870250076402, dated 08 / 28 / 2025, page 20 / 136 13 / 106 raw material containing particulate carbon.

[0045] Preferably, the amount of particulate plastic raw material in the particulate carbon-containing raw material is 20 to 100% by weight, such as 40 to 100% by weight, 50 to 99% by weight, 60 to 95% by weight, or 80 to 90% by weight, based on the total weight of the particulate carbon-containing raw material.

[0046] The feedstock for particulate biomass-based carbon black may comprise a plant-based feedstock, preferably a non-edible plant-based feedstock and / or a waste plant-based feedstock. As used in this document, the term non-edible refers to materials unsuitable for human consumption. The term waste refers to materials that are discarded or disposed of as unsuitable or no longer useful for their intended purpose, for example, after use.

[0047] The raw material for particulate biomass-based carbon black may comprise wood, grass, cellulose, hemicellulose, lignin and / or natural rubber.

[0048] As used herein, the term wood refers to the porous, fibrous structural tissue found in the stems and roots of trees and other woody plants. Suitable examples of wood include, but are not limited to, pine, fir, larch, juniper, ash, hornbeam, birch, alder, beech, oak, fir, chestnut, mulberry, or mixtures thereof. Suitable examples of grasses include, but are not limited to, cereal grasses such as maize, wheat, rice, barley, or millet; bamboos and grasses of natural fields and species cultivated in lawns and pastures. Suitable examples of lignin may include, but are not limited to, lignin removed by the Kraft process and lignosulfonates.

[0049] The rubber pellet may be composed of natural rubber and / or synthetic rubber. The raw material containing carbon particles may be composed of rubber granules containing ne Petition 870250076402, dated 08 / 28 / 2025, p. 21 / 136 14 / 106 grain of smoke. Natural rubber can be derived from rubber trees (Helvea brasiliensis), guayule, and dandelion. Rubber granules or raw material containing carbon particles can be derived from tires, cable coatings, pipes, conveyor belts, shoe soles, hoses, or mixtures thereof.

[0050] Synthetic rubber may include styrene-butadiene rubber, such as styrene-butadiene emulsion rubber (ESBR) and styrene-butadiene solution rubber (SSBR), polybutadiene, polyisoprene, ethylene-propylene-diene rubber (EPDM), ethylene-propylene rubber (EPM), butyl rubber, halogenated butyl rubber, chlorinated polyethylene, chlorosulfonated polyethylene, acrylonitrile-butadiene rubber, hydrogenated acrylonitrile-butadiene rubber, polychloroprene, acrylate rubber, ethylene-vinyl acetate rubber, ethylene-acrylic rubber, epichlorohydrin rubber, silicone rubber, fluorosilicone rubber, fluorocarbon rubber, or a mixture or combinations thereof.

[0051] Granulated or particulate plastic raw material can be any plastic known in the field. For example, acrylics, such as poly(acrylic acid) or poly(methyl methacrylate), polyesters, such as polyethylene terephthalate or polyethylene glycol, polyurethanes, such as toluene diisocyanate (TDI) derivatives or methylene diphenyl diisocyanate, polyolefins, such as polypropylene, polyethylene or polystyrene. Generally, thermoplastics and thermosets can be used.

[0052] Plastic granules are preferably sourced from household waste, such as plastic bags, plastic containers, plastic packaging, etc.

[0053] The raw material is supplied as particulate. This can be done by grinding to the desired particle size or granulate. For example, tires can be ground to obtain particulate rubber granules as raw material. Petition 870250076402, dated 08 / 28 / 2025, page 22 / 136 15 / 106

[0054] It is desired that at least 50% by weight, preferably at least 60% by weight, more preferably at least 70% by weight, most preferably at least 80% by weight, of the particulate carbon-containing feedstock have a particle size of 125 µm to 2 mm, preferably 125 µm to 1 mm, more preferably 250 µm to 1 mm and most preferably 500 µm to 1000 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[0055] It is desirable that at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the particulate carbon-containing feedstock have a particle size smaller than 2 mm, preferably smaller than 1 mm, more preferably smaller than 500 µm and most preferably smaller than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[0056] It is desirable that at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the particulate carbon-containing feedstock have a particle size smaller than 500 µm, wherein particle size is measured in accordance with ASTM D 1511-12 2017).

[0057] It is desirable that at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the particulate carbon-containing feedstock have a particle size smaller than 1 mm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[0058] It is desirable that at least 70% by weight, preferably at least 80% by weight, more preferably at least Petition 870250076402, dated 08 / 28 / 2025, page 23 / 136 16 / 106 90% by weight, more preferably at least 98% by weight, of the raw material containing particulate carbon has a particle size smaller than 2 mm, preferably smaller than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[0059] It is desirable that less than 1% by weight, preferably at least 0.5% by weight, more preferably less than 0.1% by weight, more preferably less than 0.01% by weight, of the particulate carbon-containing feedstock have a particle size greater than 2 mm, preferably greater than 1 mm, more preferably greater than 500 µm and more preferably greater than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[0060] It is particularly preferable that the raw material containing particulate carbon have a particle size smaller than 2 mm, preferably smaller than 1 mm, more preferably smaller than 500 µm and most preferably smaller than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[0061] The particle size of the feedstock can be controlled by classifying the feedstock containing carbon particles before its injection into the reactor. Consequently, it is preferable that the feedstock containing carbon particles be classified before its injection into the reactor or before its injection into the mixing and feeding unit.

[0062] Classification can be performed by any means known in the art, such as sieving or other classifications. Classification can be done using vibrating screens, rotary screens, cyclones, elutriation classifiers, air jet screens and / or dynamic air classifiers. Any of the combinations Petition 870250076402, dated 08 / 28 / 2025, page 24 / 136 The 17 / 106 classification mentioned above can be used. This classification can be used to obtain a desired maximum or minimum particle size, as described in the descriptive report.

[0063] The particle size of the feedstock can be controlled by sieving the feedstock containing carbon particles before its injection into the reactor. The sieve sizes described in ASTM D 1511-12 2017 can be used. For example, a sieve with openings of 2,000 μm, 1,000 μm, 500 µm, 250 µm or 125 µm, preferably 500 µm, 250 µm or 125 µm, can be used. In addition, the sieve can have openings with a size that retains particles larger than 2,000 µm, larger than 1,000 µm, larger than 500 µm, larger than 250 µm or larger than 125 µm, preferably larger than 500 µm, larger than 250 µm or larger than 125 µm.

[0064] Not more than 10% by weight, preferably not more than 5% by weight, more preferably not more than 4% by weight and more preferably not more than 2% by weight of the raw material containing particulate carbon must have a particle size greater than 4 mm, preferably more than 2 mm, more preferably more than 1 mm and more preferably more than 0.5 mm, where particle size is measured in accordance with ASTM D 1511-12 2017).

[0065] Not more than 10% by weight, preferably not more than 5% by weight, more preferably not more than 4% by weight and more preferably not more than 2% by weight of the particulate carbon-containing raw material shall have a particle size less than 150 µm, preferably less than 125 µm, more preferably less than 110 µm and more preferably less than 100 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017). Petition 870250076402, dated 08 / 28 / 2025, p. 25 / 136 18 / 106

[0066] None of the particles of the particulate carbon-containing feedstock shall have a particle size of 1 mm or more, preferably 500 μm or more, more preferably 250 μm or more, and most preferably 125 μm or more, where particle size is measured in accordance with ASTM D 1511-12 2017).

[0067] The particle size distribution of the particulate carbon-containing feedstock can be measured in accordance with ASTM D 1511-12 2017) and (a) sieve no. 10 retains 1 to 10% by weight, preferably 1 to 8% by weight, more preferably 1 to 5% by weight and, most preferably, 1 to 3% by weight of the particulate carbon-containing feedstock and / or (b) sieve no. 18 retains 1 to 25% by weight, preferably 2 to 20% by weight, more preferably 4 to 15% by weight and, most preferably, 5 to 12% by weight of the particulate carbon-containing feedstock and / or (c) sieve no. 35 retains 10 to 80% by weight, preferably 15 to 70% by weight.(d) sieve no. 60 retains 5 to 70% by weight, preferably 10 to 60% by weight, more preferably 15 to 50% by weight, and more preferably 20 to 45% by weight of the raw material containing particulate carbon, and / or (e) sieve no. 120 retains 1 to 80% by weight, preferably 7 to 70% by weight, more preferably 5 to 60% by weight, and more preferably 7 to 50% by weight of the raw material containing particulate carbon, and / or (f) the lower receiving tray comprises less than 4% by weight, preferably less than 3% by weight, more preferably 0 to 2% by weight and, preferably, of 0.01 to 1% by weight of the raw material containing particulate carbon. It is desirable to choose the desired range for each sieve accordingly. Petition 870250076402, dated 08 / 28 / 2025, page 26 / 136 19 / 106 dependent.

[0068] The cumulative particle size of 50% by weight of the particulate carbon-containing feedstock shall be 100 μm to 4 mm, preferably 100 μm to 3 mm, more preferably 100 μm to 2 mm, and even more preferably 100 μm to 500 μm, the cumulative particle size of 50% by weight being measured in accordance with ASTM D 1511-12 2017). The cumulative particle size of 50% by weight may be interpolated using standard techniques known in the field. It is particularly preferable that the Rosin-Rammler-Sperling-Bennett distribution (RRSB distribution) be used to interpolate the cumulative particle size of 50% by weight.

[0069] The weight-average particle size Dw50 of the particulate carbon-containing feedstock may be from 100 μm to 4 mm, preferably from 100 μm to 3 mm, more preferably from 100 μm to 2 mm, and most preferably from 100 μm to 500 μm, wherein the weight-average particle size Dw50 is measured in accordance with ASTM D 1511-12 2017).

[0070] The Dw10 particle size distribution of the particulate carbon-containing feedstock may be from 100 μm to 250 μm, preferably from 110 μm to 220 μm, more preferably from 120 μm to 210 μm and, most preferably, from 130 μm to 200 μm, wherein the Dw10 particle size distribution is measured in accordance with ASTM D 1511-12 2017).

[0071] The particle size distribution of the Dw90 particulate carbon-containing feedstock may be from 400 μm to 4 mm, preferably 500 μm to 3 mm, more preferably 600 μm to 2 mm and most preferably 700 μm to 500 μm, wherein the Dw90 particle size distribution is measured in accordance with ASTM D 1511-12 2017). Petition 870250076402, dated 08 / 28 / 2025, page 27 / 136 20 / 106

[0072] The range of particle size distributions of the particulate carbon-containing raw material (Dw90-Dw10) / Dw50 may be 0.2 to 1.8, preferably 0.3 to 1.3, more preferably 0.4 to 1.1, most preferably 0.4 to 1.0, wherein the Dw10, Dw50 and Dw90 particle size distributions are measured in accordance with ASTM D 1511-12 2017).

[0073] Dw50, Dw10 and Dw90 can be interpolated using standard techniques known in the field. It is particularly preferable that the Rosin-Rammler-Sperling-Bennett distribution (RRSB distribution) be used to interpolate Dw50, Dw10 and Dw90.

[0074] The size of the particles or granules influences the heating rate of the feedstock in the reactor. Smaller granules or particles have a larger specific surface area, resulting in a higher heating rate. A rapid heating rate is beneficial so that the particulate feedstock can evaporate and then be pyrolyzed. Pyrolysis is believed to be significantly faster than the evaporation of the particulate feedstock. The heating rate can also be increased by a higher temperature of the hot gas stream.

[0075] Carbon black produced according to the present invention (such as the inclusion of rCB) and / or feedstock containing particulate carbon may have a pMC (percentage of modern carbon) of 1% or higher, determined in accordance with ASTM D6866-20 Method B (AMS), as 2% or higher, or 5% or higher, or 7% or higher, or 10% or higher, or 12% or higher, or 15% or higher, or 17% or higher, or 20% or higher, or 22% or higher, or 25% or higher, or 27% or higher, or 30% or higher, or 32% or higher, or 35% or higher, or 37% or higher, or 40% or higher, or 42% or higher, or 45% or higher, or 47% or higher, or 50% or higher, or 52% or higher, or 55% or higher, or 57% or higher, Petition 870250076402, dated 08 / 28 / 2025, page 28 / 136 21 / 106 or 60% or higher, or 62% or higher, 65% or higher, or 67% or higher, or 70% or higher, or 72% or higher, or 75% or higher, or 77% or higher, or 80% or higher, or 82% or higher, or 85% or higher, or 87% or higher, or 90% or higher, or 92% or higher, or 95% or higher, or 97% or higher, or 99% or higher. For each sample, a 14C / 13C ratio is calculated and compared with measurements made with the oxalic acid II standard (NIST-4990C). The measured values ​​(pMC) are corrected for the 13C measured using an isotope ratio mass spectrometer (IRMS). The carbon black of the present invention may have a pMC (percentage of modern carbon) of 5% or higher, determined in accordance with ASTM D6866-20 Method B (AMS), preferably 10% or higher, particularly preferably 15% or higher, more preferably 50% or higher, even more preferably 85% or higher, even more preferably 90% or higher.The carbon black of the present invention may have a pMC (percent modern carbon) of 100%, determined in accordance with ASTM D6866-20 Method B (AMS) standard.

[0076] The carbon black obtained typically comprises recovered carbon black and new carbon black. Recovered carbon black is generally obtained if the raw material containing carbon particles is composed of carbon black. New carbon black is obtained by pyrolysis, i.e., the method according to the invention.

[0077] The mass flow rate of the feedstock must be adjusted so that the feedstock can be heated uniformly. The feedstock containing particulate carbon should be injected into the reactor at a mass flow rate of 2 to 50 kg / h per 130 L of reactor reaction volume, preferably 5 to 40 kg / h per 130 L of reactor reaction volume, more preferably 8 to 30 kg / h per 130 L of reactor reaction volume, and even more preferably 10 to 20 Petition 870250076402, dated 08 / 28 / 2025, page 29 / 136 22 / 106 kg / h per 130 L of reactor reaction volume.

[0078] The fuel may comprise gaseous or liquid hydrocarbons, preferably natural gas, fuel oil or H2.

[0079] Hydrogen can be used as a carrier gas and / or fuel for the production of carbon black. It is preferable that hydrogen be used as both a carrier gas and fuel for the production of carbon black. Hydrogen will be used as a carrier gas if hydrogen is present in the combustion mixture in molar excess relative to oxygen. Therefore, hydrogen must be present in the hot combustion gases and in the hot reaction mixture.

[0080] The hot gas stream must have a temperature of 900 to 3500°C, preferably from 950 to 3000°C, more preferably from 1000 to 2000°C, and most preferably from 1200 to 1900°C.

[0081] Hot gas flow can be obtained by electric preheating, plasma, and combustion of a fuel gas containing oxygen. Combustion of a fuel gas containing oxygen is preferably carried out in a furnace reactor. However, other means of providing the desired temperature of the hot gas flow are possible, as mentioned above.

[0082] The entrained flow reactor can be a furnace reactor. A furnace reactor may have a flow passage along a central longitudinal axis of the reactor. The reactor generally comprises, in the following order, from upstream to downstream (flow direction), a combustion chamber, a choke point, and a tunnel with quenching media. These components define a flow passage along the central longitudinal axis of the reactor for the flow of hot gas, such as hot combustion gases. Therefore, the components must be in fluid connection, particularly along a central longitudinal axis of the reactor. Petition 870250076402, dated 08 / 28 / 2025, page 30 / 136 23 / 106

[0083] A tubular conduit may be connected to the combustion chamber to supply the oxygen-containing gas necessary for fuel combustion (or combustion fuel). The tubular conduit may also be arranged along the central longitudinal axis of the reactor, so that the supply of oxygen-containing gas occurs along the flow passage mentioned above. In addition, the reactor may comprise fuel injection devices to inject fuel into the combustion chamber.

[0084] Generally, a fuel lance is used to supply fuel to the combustion chamber. The combustion chamber may be connected to the tubular conduit in a downstream-to-upstream direction so that oxygen-containing gas can be supplied to the combustion chamber. The combustion chamber is arranged along the central longitudinal axis of the reactor.

[0085] The combustion chamber is preferably formed by an inner refractory lining covered by a gas-tight metal cover, for example. The material forming the refractory and the outer lining can be those conventionally found in the art, such as the moldable refractory Kaocrete® 32 cm, which is composed of 70% alumina (Al2O3) and has a melting point of about 1870°C. Alternatively, a brick refractory can be used, such as RUBY SR (sold by Harrison-Walker Refractories, Pittsburg, PA), which is composed of 84.5% alumina and 9.8% chromium oxide (Cr2O3) and has a melting point of about 2050°C. The casing or lining is preferably made of carbon steel, except for any piping in contact with the hot process air. In these areas, the piping is made of 316 stainless steel.

[0086] The combustion chamber is preferably dimensioned as a cylinder. A constriction (throttling) section may be provided downstream of the combustion chamber. The constriction section Petition 870250076402, dated 08 / 28 / 2025, page 31 / 136 24 / 106 The section has a conical passage and converges in the upstream-to-downstream direction. Preferably, these constriction sections have the shape of a truncated conical passage. The combustion chamber may also have a conical passage in the downstream-to-upstream direction. Consequently, the combustion chamber may comprise a zone that is conical towards the reaction chamber and / or towards the tubular conduit.

[0087] Normally, the oxygen-containing gas is preheated to a temperature between 200 and 1600°C, preferably 350 and 1400°C, more preferably 500 and 1200°C and most preferably 450 and 950°C.

[0088] Normally, the fuel is preheated to a temperature between 50 and 750°C, preferably 100 to 700°C, more preferably 300 to 700°C and most preferably 450 to 650°C.

[0089] Preheating of gas and oxygen-containing fuel can be done electrically or using a heat exchanger.

[0090] Water influences the surface properties of the carbon black produced. Consequently, it is possible that the amount of oxygen-containing gas, such as O2, in the combustion mixture can be used to control the amount of water in the hot combustion mixture and / or the hot reaction mixture, and thus preferentially control the surface properties of the carbon black produced.

[0091] The tunnel is connected to the combustion chamber so that the hot combustion gases obtained in the combustion chamber can flow into the tunnel. The tunnel can be arranged along the central longitudinal axis of the reactor. The diameter of the reaction chamber can be larger than the diameter of the constriction section of the combustion chamber, so that the hot combustion gas can expand. The expansion section is preferably dimensioned as a cylinder and in communication with the combustion chamber, preferably Petition 870250076402, dated 08 / 28 / 2025, page 32 / 136 25 / 106 mind in communication with the constriction (throttling) section of the combustion chamber.

[0092] The feedstock containing carbon particles can be injected into the combustion chamber, at the choke point and / or in the reactor tunnel of the furnace. The feedstock containing carbon particles is typically injected at the choke point (constriction section).

[0093] If the feedstock containing carbon particles is injected, for example, into the combustion chamber, the feedstock containing carbon particles or the carrier gas that composes it must have a desirable pressure. This means that the pressure of the feedstock containing carbon particles or the carrier gas that composes it must be greater than the pressure in the combustion chamber. Consequently, a suitable feeding and mixing device must be used, configured to operate under pressurized conditions.

[0094] The feedstock containing particulate carbon should be injected through multiple inlets, preferably radial and perpendicular to the central longitudinal axis of the reactor.

[0095] The O2 concentration in the hot gas stream should be less than 5% by volume, preferably less than 4% by volume, more preferably from 0.01 to 3% by volume and, most preferably, from 0.1 to 2% by volume.

[0096] The carbon black obtained generally comprises recovered carbon black and new carbon black.

[0097] Raw material containing carbon particles can be injected into the reactor by means of injection devices. The injection devices may comprise a plurality of nozzles or injection lances, preferably arranged circumferentially with respect to the central longitudinal axis. The circumferential arrangement further improves the uniform characteristics of the carbon black, since the Petition 870250076402, dated 08 / 28 / 2025, p. 33 / 136 26 / 106 raw material for carbon black can be homogeneously mixed with a hot gas stream. The raw material containing carbon particles can be introduced using a plurality of injection devices.

[0098] For example, an axially extending feedstock lance and radially extending feedstock injectors with nozzles capable of producing a variety of cone-shaped sprays (e.g., cone spray angles of 15, 30, 45 and 60 degrees) can be implemented.

[0099] To produce the desired characteristics of carbon black, radially extending feedstock injectors can be fitted with shut-off valves, so that feedstock is introduced only through certain feedstock injectors or that the flow rate of feedstock flowing through the injectors is varied.

[00100] The means for injecting the raw material is preferably connected to a feeding and mixing device. It is desirable that a feeding and mixing device provides multiple raw material inputs. However, it is also possible that more than one feeding and mixing device is used.

[00101] The tunnel may further comprise means for injecting a quenching medium into the flow passage along the central longitudinal axis of the reactor, located downstream of the flow direction, to inject a feedstock for carbon black. Alternatively, the quenching medium may be a quenching boiler or a heat exchanger.

[00102] The tunnel may comprise means for injecting a quenching medium into the flow passage along the central longitudinal axis of the reactor. The means for injecting a quenching medium are located subsequently, in relation to the flow direction, to the means for in Petition 870250076402, dated 08 / 28 / 2025, page 34 / 136 27 / 106 to jet a raw material for carbon black. The quenching medium is usually H2O.

[00103] The distance between the raw material injection medium and the medium for injecting a quenching medium (the first medium for injecting a quenching medium) may be between 150 and 80,000 mm, preferably 900 and 50,000 mm, more preferably 1,500 and 30,000 mm and, most preferably, 2,500 and 20,000 mm.

[00104] The means for injecting a quenching medium may extend into the tunnel. For example, a cooling fluid conduit or a plurality of radial cooling fluid conduits may be used. The quenching medium, such as a cooling fluid (e.g., water), may be sprayed inside the tunnel to stop the carbon black reaction at the appropriate time and place.

[00105] The reactor may also comprise a tubular conduit to supply oxygen-containing gas to the combustion chamber. The oxygen-containing gas (O2-containing gas or a mixture of O2-containing gases) may be air, oxygen-enriched air, other oxygen-containing gases, and / or pure oxygen. Consequently, the tubular conduit may be connected to the combustion chamber so that the oxygen-containing gas can flow through the tubular conduit into the combustion chamber. The tubular conduit may be arranged along the central longitudinal axis of the reactor. It is desirable that the central longitudinal axis of the tubular conduit be coaxial to the central longitudinal axis of the reactor. Thus, the tubular conduit may be arranged coaxially along the central longitudinal axis of the reactor.The percentage by weight of oxygen present in the oxygen-containing gas should be from 20 to 100% by weight, preferably from 50 to 99% by weight, more preferably from 60 to 95% by weight, and even more preferably from 70 to 90% by weight, where the percentage by weight is based on the total weight of the oxygen-containing gas. Petition 870250076402, dated 08 / 28 / 2025, page 35 / 136 28 / 106

[00106] The tubular conduit may have a cylindrical shape that extends along the central longitudinal axis of the reactor without bends.

[00107] The internal diameter of the tubular conduit for supplying oxygen-containing gas may be 5 cm to 3 m, as well as 10 cm to 3 m, 20 cm to 3 m, 9 cm to 2.5 m, 13 cm to 1.5 m, 0.1 m to 2 m, 20 cm to 1 m, 30 cm to 1.5 m, 15 cm to 60 cm or 15 cm to 90 cm.

[00108] Fuel injection means for introducing any suitable combustion fuel (e.g., natural gas, fuel oil, or other gaseous or liquid hydrocarbons, preferably natural gas or fuel oil, or H2) may be configured in different ways. For example, the injection means may be arranged at the end of the tubular conduit where the tubular conduit is connected to the combustion chamber. For example, the injection means are tubular injection tubes arranged circumferentially with respect to the central longitudinal axis of the tubular conduit, so that the fuel injection angle is substantially orthogonal to the direction of flow of the oxygen-containing gas.

[00109] However, it is also possible to provide multiple fuel injection means in addition to the fuel lance. For example, at the end of the tubular conduit, additional fuel injection means are arranged rotationally symmetrically with respect to the central longitudinal axis of the tubular conduit.

[00110] The oxygen-containing gas is generally supplied in an amount that produces an excess of oxygen relative to the amount of oxygen for complete combustion of the fuel, and / or wherein the oxygen-containing gas is supplied in an amount wherein the value k is in a range of 0.01 to 10, preferably 0.1 to 5, more preferably 0.5 to 2, and even more preferably 0.7 to 1. Wherein the value k is defined by the ratio between the stoichiometric amount of O2 required for complete combustion and the amount of oxygen supplied. Petition 870250076402, dated 08 / 28 / 2025, page 36 / 136 29 / 106 complete fuel exchange and the amount of O2 supplied.

[00111] The fuel gas and oxygen flow rates can be adjusted to generate high temperatures and typically approach stoichiometric ratios. The ratios must be adjusted to prevent refractory melting. The oxygen gas flow rate range is quite wide, varying, for example, from a minimum value of approximately 1000 Nm3 / ha to a maximum value of approximately 100 kNm3 / h, such as 1000 Nm3 / ha 100 kNmP / h, 1000 Nm3 / ha 10 kNm3 / h, 2000 Nm3 / ha 3000 Nm3 / h or 1000 NmP / ha 2000 NmP / h. The invention, however, is not limited to these dimensions; for larger reactors, higher air flow rates are required, and for smaller reactors, lower air flow rates.

[00112] The desired temperature of the hot gas stream can also be achieved by plasma heating. The gas stream can be preheated as mentioned above.

[00113] A plasma torch can provide the plasma for the aforementioned heating. A plasma torch design is described in WO 1993 / 012633 A1. However, any means known in the art for producing plasma can be used. The plasma can be formed by means of a plasma carrier gas, which is heated by an electric arc burning between the electrodes. In a plasma zone, high temperatures are reached, from 2500°C to 20,000°C, and it is in this zone that plasma treatment can be performed. The plasma carrier gas can be oxygen or hydrogen. Hydrogen as a plasma carrier gas is particularly preferred.

[00114] A microwave plasma can also be used for the aforementioned treatment. For example, a microwave generator can be used to provide microwave radiation within the reaction chamber. Microwave radiation from 1 to 300 GHz can be used. Alternatively, a plasma can be generated using a source of Petition 870250076402, dated 08 / 28 / 2025, page 37 / 136 30 / 106 radio frequency energy (RF generator).

[00115] The residence time between the moment of injection of the feedstock containing particulate carbon into the reactor and the cooling time of the product mixture should be 150 ms to 4 s, preferably 200 ms to 3 s, more preferably 250 ms to 2 s, and even more preferably 250 ms to 1 s. The residence time of the feedstock containing particulate carbon means the time during which the feedstock containing particulate carbon is evaporated and pyrolyzed. Cooling of the product mixture stops the pyrolysis of the feedstock containing particulate carbon. The heating rate of the feedstock containing particulate carbon is lower compared to that of liquid feedstocks, so the evaporation and pyrolysis of the feedstock containing particulate carbon generally require more time.

[00116] The residence time of the raw material containing particulate carbon should be 150 ms to 4 s, preferably 200 ms to 3 s, more preferably 250 ms to 2 s, and even more preferably 250 ms to 1 s, the residence time being calculated according to equation (1); V Equation (1), where t is the residence time, V is the reaction volume (in m3) and Q is the volumetric flow rate (in m3*s'1).

[00117] The volumetric flow rate is the volume of fluid after injection of the raw material containing particulate carbon into the hot gas stream per second, preferably the fluid volume is calculated according to the ideal gas law according to equation (2) ÚRT Equation (2), Petition 870250076402, dated 08 / 28 / 2025, page 38 / 136 31 / 106 where Q is the fluid volume flow rate (in m3*s'1), ri is the sum of the molar flow rates of gaseous substances N2, CO2, CO, H2O, volatiles (in ms-1), R is the gas constant, i.e., 8.3145 JK“1mol“1, T is the absolute temperature, P is the pressure. The pressure P can be measured in the reactor or, alternatively, 103125 Pa is used for the calculation. For ri and the amount of substance, all substances are considered to be in the gaseous state (including the feedstock containing particulate carbon). The volatiles are the volatiles of the feedstock containing particulate carbon measured according to ASTM D4530-15 2020). For the molecular weight of the volatiles, 198 g / mol can be used. The components of the hot gas flow are calculated considering the complete combustion of the fuel. For the remaining oxygen, it is considered that the oxygen reacts with the carbon-containing material, assuming that one O2 results in one H2O and one CO2.The calculation considers the fluid (for volumetric flow calculation) after the injection of the carbon-containing feedstock into the hot gas stream, and that the carbon-containing part of the feedstock is completely in the gaseous state. Materials that are not in the gaseous state are not considered. Furthermore, the pyrolysis of the carbon-containing part of the feedstock is not considered in the calculation. An example of the calculation is specified in the description and can be adapted to the specific method of carbon black manufacturing.

[00118] The reaction volume of the reactor is the volume of the reactor between the injection position of the feedstock containing carbon particles and the cooling position.

[00119] The residence time must be selected so that the C,H-containing material in the particulate carbon-containing feedstock is completely pyrolyzed.

[00120] The absolute temperature for calculating the volumetric flow rate can be measured directly in the reactor. In particular, the temperature is Petition 870250076402, dated 08 / 28 / 2025, page 39 / 136 32 / 106 measured immediately after the raw material is injected into the reactor, for example, 50 mm after injection. For example, the temperature can be measured with a pyrometer.

[00121] Alternatively, the absolute temperature T (for volumetric flow rate calculation) can be calculated as follows. This calculation considers the combustion of a fuel in a furnace reactor. The process involves the combustion of the fuel and the heating of the rubber granules to the reaction temperature. The residual oxygen from the combustion will not lead to complete combustion. Therefore, it can be assumed that, according to the C / H ratio of the raw material, CO and H2O will be formed with the same CO / H2O ratio.

[00122] The reaction temperature can be calculated by the energy balance = mF(hF+ HuF) +Σ£=1™,A + mT{hT+ HuT)+mR(hR+—= — Qpgr^a Equation (3)

[00123] The fuel mass flow rate is denoted by mF, hF is the thermal enthalpy difference between the temperature and pressure at the fuel inlet of the combustor and the fuel reference conditions (T = 25°C, P = 101325 Pa), mA is the mass flow rate of inert species and hA is the specific thermal enthalpy difference of the inert species A between 25°C and 1.01325 bar and the conditions of the inert species being introduced into the combustor (TA, PA). The number of inert substances is denoted by K. Inert species are species that are not altered in the ideal process. These inert substances are, for example, nitrogen, carbon black and minerals, water. &HuF is the lower calorific value of the fuel at a temperature of 25°C and a pressure of P = 101325 Pa. The thermal enthalpy difference of oxygen between the feed conditions and the reference conditions (T = 298.15 K, P = 101325 Pa) is denoted by h0? and the flow rate of Petition 870250076402, dated 08 / 28 / 2025, page 40 / 136 33 / 106 The mass of oxygen is denoted by fk. The specific thermal enthalpy difference of the reaction product i between the reaction temperature condition T and P = 101325 Pa and the reference conditions (T = 298.15 K, P = 101325 Pa) is denoted by λ. The corresponding mass flow rate is denoted by mp^e and the lower heating value of this compound is denoted by Hui. If the particle-containing feedstock is transported with a gas stream into the reactor, this gas mass flow rate is denoted by mr, the thermal enthalpy difference between the condition at the reactor inlet and the reference condition (T = 25°C, P = 103125 Pa) of this mass flow rate is denoted by (hT, and HuT is the corresponding lower specific heating value. Heat losses are considered by Qloíj. The mass flow rate of the hydrocarbon part of the particle-containing carbon is denoted by mR and can be calculated by mR = -ω - Conradson). The mass flow rate of the feedstock containing particulate carbon is denoted by ms. The thermal enthalpy difference of the hydrocarbon between the inlet state and the reference state (T = 25°C, P = 101325 Pa) is given by hR, and the corresponding lower heating value by / / uH.

[00124] The lower heating value is determined according to DIN 5499 and DIN 51857 standards. If the gases are not listed in DIN 51857, the lower heating value can be determined from the Properties of Gases and Liquids, in the NIST Data Book, etc., based on the assumption of complete oxidation of the CxHySzOwe species of gaseous water as a reaction product. CxHySzOwAp+ vo?O2= xC02+ —H2O + zS0? + eAf Equation (4)

[00125] Where A is a non-oxidized substance. Ã^A is substance A in the form of A in the combustion product. Therefore, p = fe. Petition 870250076402, dated 08 / 28 / 2025, page 41 / 136 34 / 106 The heating value is ^^HyS^Ap =— ™CxHySsOwAp — XÁf HCCj2(Tjçg.is)—¢^298,15)-^¾¾ ¢^298,15^ — eA^HCOq(7^98,15)) Equation (5)

[00126] If the reference temperature for the heat of formation is different from 298.15 K for a substance i, the heat can be calculated using the molar heat capacity ^298.15 A' ^^¢^298.15^—TI ^mp,í ^ref Equation (6)

[00127] Molar heat capacity can be found using the same textbooks, such as Properties of Gases and Liquids and the NIST Databook.

[00128] If the fuel is composed of more than one species, the lower calorific value can be determined by the composition p í=l Equation (7)

[00129] The mass fraction of component I is denoted by the lower heating value of component i is denoted by ΔH^ρ and the number of species in the fuel is denoted by P.

[00130] The thermal enthalpy difference of the fuel containing more than one species is calculated by pT^F=77 / Xí I ^mp,i *'F ^298,15 K Equation (8)

[00131] The average molecular weight of the fuel is determined by Petition 870250076402, dated 08 / 28 / 2025, page 42 / 136 35 / 106 Equation (9) M,- is the molecular weight of species i.

[00132] If the composition is unknown, the lower heating value is determined by a calorimeter. If the fuel is solid or liquid, the lower heating value is determined according to DIN 51900. From the experimental results, the water content should be measured according to ASTM D 4928-12 2018, and the sulfur content and hydrogen content were measured according to the method described in the examples.

[00133] The difference in thermal enthalpy of the combustion gases between T=298.15 K and the flame temperature by N „ I V-1ΓJnriinbnr ^Gos=Tf / N í Ujíf.,! dT '^Gas 77^J29S,15 λ' Equation 10)

[00134] The number of species in the product gas stream is denoted by N, the average molecular weight of the combustion gas is denoted by MGit;, the average molecular weight is determined by 1Mcas'EU Equation (11)

[00135] The lower heating value of inert species in the product stream is defined as 0 J / mol.

[00136] To determine the lower heating values ​​of the hydrocarbon-containing species in the particulate feedstock, it is necessary to determine the water content (ASTM D 4928-12 2018) and the Micro Conradson content according to ASTM D4530-15 2020). Furthermore, the final analysis of the particulate feedstock must be measured according to ASTM D3176-15 2016) and the gross calorific value of Petition 870250076402, dated 08 / 28 / 2025, page 43 / 136 36 / 106 in accordance with ASTM D 4809:2018.

[00137] The lower heating value of the particulate raw material is calculated by H^s (Has 3“91 / (1 — w)

[00138] Furthermore, it is possible to determine the lower heating value of the Conradson residue by measuring the higher heating value and hydrogen content of the Conradson residue using the same equation. The water content of the Conradson residue is 0. The lower heating value of the hydrocarbon containing particles is determined by Hur = — w) — HuCaju.adsanConradson) / (I — w — Conradson)

[00139] To determine the C / H ratio of the hydrocarbon portion, one can obtain from the final analysis of the particulate raw material and the final analysis of the Conradson £ _ 1 [c / 1 - w) - Conradson cConradson] H 12 [Λ,(1 - w) - Conradson hrn„rnrí^n„]

[00140] The molar enthalpy difference for water can be determined by / 102318^7 II hr = ---ζ4ΐη7^ - 0109--7 + 33 25--—(T - 298.15 / 0 u.vr'4iJ2' 1 molK \ exp — 7* z J Equation (12)

[00141] For CO2 we obtain I 56385 —7 ir hco= ------ 191.89---+ 29.10---(7-298.15 / 03l O69S*0 1 mol molK i exp — 7* z J / ^co2 Equation (13)

[00142] For SO2 Petition 870250076402, dated 08 / 28 / 2025, p. 44 / 136 37 / 106 34594 _____mol (1387KX 'IT / / ^so^ 333.37---+ 33.26-----(,T - 298.15 / 0 mol molK Equation (14)

[00143] For N2 (27423_______mol / 329871, exp — J - 1 / ¾ 0.43-- + 29.10 mol ----(T - 298.15 / 0 mo IK

[00144] For 02 Equation (15) / 17808^7 _ I ________mol I <214171 , \ exp —) — 1 13.52 + 29.10 —— (T - 298.15ff) mol molK Equation (16)

[00145] For CO 1-^ + 29.10—^(7-298.15 / 0 mol molK co Equation (17)

[00146] The lowest heating value of CO₂ is Hu / C₀ = 282980

[00147] For gaseous rubber products ^Rubber 2218695 mol 1976K T 2933-^7 + 33.25<7 - 298.157) mol molK V + 500 — kQ 0.212-¾ mol Equation (18) Petition 870250076402, dated 08 / 28 / 2025, page 45 / 136 38 / 106

[00148] For particulate rubber we obtain hBarracha,s= 1960 / / WT -298.15 K) Equation (19)

[00149] For Conradson Equation (20) Exemplary calculation

[00150] Combustion of methane entering the combustion chamber at 3 bar and a temperature of T=290 K

[00151] Having a standard methane volume flow rate considering a pressure of 101325 Pa and a temperature of T=273.15K of 13 Nm3 / h (STP) and nitrogen with a temperature of T=673.15 K and a pressure of 1.2 bar having a standard volume flow rate of 118.5 Nm3 / h (STP) considering a pressure of 101325 Pa and a temperature of T=273.15K and a standard oxygen flow rate of 31.5 Nm3 / h (STP) referring to the standard temperature of T=273.15 K and a standard pressure of P=101325 Pa.

[00152] In the throttling, a mass flow rate of 20 kg / h of rubber granules is dosed to the system with a temperature of 20°C and a pressure of 1 bar.

[00153] The lower heating value of methane, according to DIN 51857, with T = 298.15 K and P = 101325 Pa, is 802.6 MJ / kmol. In Properties of Gases and Liquids, you obtain a heat capacity for methane of Cp(T)=8.314462*(4.568-8.975 / 10Λ3*Τ+3.631 / 10Λ5*ΤΛ23.407 / 10Λ8*ΤΛ3+1.091 / 10Λ11 *ΤΛ4) Equation (22)

[00154] Therefore, h_f is obtained by Petition 870250076402, dated 08 / 28 / 2025, p. 46 / 136 39 / 106 y'Zγ-3 hf = 8.314462 * (4.568 *T- 8.975 / 10Λ3 * — + 3.631 / 10Λ5 * — 23 - 3,407 / 10Λ8* — + 1,091 / 10Λ11 * — -(4,568* Γο45 8,975 Γ023,631 %33,407 1,091 Το5 ΙΟ3* 2+ΙΟ5* 3-ΙΟ8* 4+ΙΟ11* 5 Equation (23)

[00155] The fuel supply temperature is symbolized by T and given in the example by T=290 K, the reference temperature of the heating value is given by T o =298.15 K.

[00156] The enthalpy difference between T = 298.15 K and the feed temperature can be determined by equation (4). For oxygen, it is possible to determine the enthalpy difference by equation (15).

[00157] Heat losses occur in the reactor shell according to the temperature measured in the shell. Heat transfer can be calculated following the VDI Warmlemma. Heat transfer should encompass radiation and convection / free convection.

[00158] Calculation of mass flows of compounds in the reaction zone

[00159] In Eq. (4), x-1, y-4, z-0, w-0, p-0. Therefore, we obtain, from 13 Nm3 / h of methane, 13 Nm3 / h of CO2 and 26 Nm3 / h of water. Residual oxygen is determined by the total oxygen flow minus the oxygen flow in the forms of CO2 and H2O (SO2 if there is sulfur in the fuel). The conversion between mass flow and standard volumetric flow is done for gaseous species by 771b= --------PRTa Equation (24), To is 273.15 K, P° is 101325 Pa.

[00160] Therefore, it is obtained from the remaining oxygen flow Petition 870250076402, dated 08 / 28 / 2025, page 47 / 136 40 / 106 VpH 0Nm313Nm313Nm3^PO^remaining ^Ρθ2—^Pco231.5 — — — “ Equation (25)

[00161] It is assumed that the residual oxygen is converted by the hydrogen and carbon from the rubber part of the granules in a proportion equivalent to the atomic H / C ratio of the rubber part. Assuming an H / C ratio of 2, one H2O and one CO are obtained. Therefore, it is necessary to add to the already calculated water flow the following flow rate of 5.5 Nm3 / h of H2O, obtaining a total of 31.5 Nm3 / h of H2O and 5.5 Nm3 / h of CO. The rubber granules are transported by 8 Nm3 / h of nitrogen into the reactor.

[00162] These gas flows are converted into mass flows using the equation above, resulting in: n2 158.02 kg / h co2 25,519 kg / h H2O 20.88 kg / h CO 6.87 kg / h H2Oadd 4.42 kg / h

[00163] The mass flow rate of rubber in the gas phase is calculated from the total flow rate of rubber granules subtracting the inert species and subtracting the mass flow rate of burnt rubber ™P Rubber, Res mp^ ^PGranuladodeborracha * Cl—Conradson) — 2— — JO mpco^3 - 12----= 8.96 — 28h Equation (26)

[00164] Conradson is treated as an inert material which can be calculated by ™P Conradson ^PGranuladadebarracha * (Conradson) = 7.6 — h Petition 870250076402, dated 08 / 28 / 2025, page 48 / 136 41 / 106 Equation (27) Calculation of heat loss

[00165] The heat flow can be calculated by Qím= - Tp + <TW- T„) Equation (28)

[00166] In the case of free convection, alpha is calculated by the Nusselt number, a function of the Rayleigh and Prandtl numbers, Pr. Nude and 2A 0.752 + 0.387 (fía / (Pr))6 Equation (29)

[00167] Using Equation (30)

[00168] The Rayleigh number is calculated by / d\3 9.81m 72 1 Ra =---— *--------* (Tw — Tu) * Pr S Equation (31)

[00169] By cooperating all these in the energy balance, we obtain Pc T + ^Pconradion ^Conradaont^GraniiIadüdsüorracfta^ + 'm,pBorracfiaiSÇhRubbgr(TGranuladadgj}orracfia) + ü r + ™Pn2hx2(Tair') + mp33+ mpT(hT(Tr) + HUiT) ^Pconradsonhconradson^T) + ^PBarracha^es^Rubber^T) + Hu,Borracha+) + ^Pc + ^PcO ^CO + ^uCO^ + + mPt^N^ + Qp^rda Equation (32)

[00170] The reactor has an external area of ​​15.9 m2. Therefore, a temperature of 1629°C was obtained for the given example. The reaction volume is 0.162 m3. The volumetric flow rate of all species, except mConradson's, is 1236 m3 / h. Therefore, a residence time of... Petition 870250076402, dated 08 / 28 / 2025, page 49 / 136 42 / 106 tr= —rQ Equation (1) of 0.38 s. In the last equation, the reactor volume is denoted by V and the volume flux of all species except Conradson is Q. In this example, all species except Conradson are Rubber, Res CO2COH 2ON2.

[00171] In general, the residence time is selected so that the C,H-containing material in the particulate carbon-containing feedstock is completely pyrolyzed.

[00172] Carbon black formation is generally stopped by quenching the hot gas stream. Thus, the method may further comprise (e) quenching the hot gas stream after injection, in accordance with step (d).

[00173] Transmittance can be an indicator that the residence time is sufficient for the feedstock, allowing complete pyrolysis, for example, of the C,H-containing material in the feedstock. Consequently, the hot gas flow must be quenched (e) when the transmittance at 425 nm of the carbon black obtained is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, even more preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 for toluene.

[00174] The transmittance at 425 nm of the produced carbon black can be measured and the cooling position can be adjusted until the transmittance at 425 nm of the produced carbon black is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 relative to Petition 870250076402, dated 08 / 28 / 2025, p. 50 / 136 43 / 106 toluene.

[00175] The quenching position in the entrained flow reactor may be selected such that the transmittance at 425 nm of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene.

[00176] A method is provided for adjusting the cooling position in an entrained flow reactor for the production of carbon black from a feedstock containing particulate carbon, comprising: I) injecting a feedstock containing particulate carbon into a hot gas stream of an entrained flow reactor, wherein the hot gas stream has a temperature of at least 800°C; II) cooling the hot gas stream comprising the carbon black produced; III) measuring the transmittance of the carbon black produced; IV) adjusting the cooling position in the entrained flow reactor until the transmittance of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene.

[00177] It is particularly preferable that the feedstock containing carbon particles be deagglomerated before injection into the reactor. It is believed that the evaporation time is reduced with the use of deagglomerated particles.

[00178] Consequently, it is desirable that step (b) further includes the deagglomeration of the feedstock containing particulate carbon and, in step (d), the feedstock containing particulate carbon Petition 870250076402, dated 08 / 28 / 2025, page 51 / 136 44 / 106 deagglomerated carbon is injected into the hot gas stream to form carbon black.

[00179] Thus, a method must be provided for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, comprising: (a) providing a hot gas stream, (b) deagglomerating a feedstock containing particulate carbon to provide a deagglomerated feedstock containing particulate carbon, and (d) injecting the deagglomerated feedstock containing particulate carbon into the hot gas stream to form carbon black, wherein the hot gas stream has a temperature of at least 800°C.

[00180] Deagglomeration can be achieved by (i) accelerating the feedstock containing carbon particles and / or (ii) applying shear forces, preferably using an extruder. Deagglomeration can be achieved in (i) a feeding and mixing device, preferably comprising a nozzle, and / or (ii) an extruder. The feeding and mixing device is preferably a device according to the invention.

[00181] The acceleration of the raw material containing carbon particles results in the deagglomeration of the particles. For example, a carrier gas, such as N2 or air, can be accelerated and the particles are injected into the accelerated carrier gas. In other words, deagglomeration can be achieved by subjecting the raw material containing carbon particles to a jet of carrier gas.

[00182] Deagglomeration can be carried out in (i) a feeding and mixing device comprising a Laval nozzle.

[00183] The carrier gas and / or feedstock containing carbon particles are preferably accelerated to more than 1 Ma, preferably from 1.01 Ma to 1.7 Ma, more preferably from 1.1 Petition 870250076402, dated 08 / 28 / 2025, p. 52 / 136 45 / 106 From 1.6 Ma to 1.6 Ma, and even more preferably from 1.2 Ma to 1.5 Ma. A Mach number greater than 1 can be obtained with a jet nozzle, such as a Laval nozzle. Ma is the Mach number.

[00184] Meanwhile, flow velocities of 0.01 Ma to 3 Ma, preferably 0.1 Ma to 2 Ma, more preferably 0.2 to 1.8 Ma and most preferably 0.3 to less than 1 Ma, are also desirable.

[00185] Deagglomeration is also achieved by impacting the accelerated feedstock containing particulate carbon with an object, such as two particles of the feedstock containing particulate carbon, or by impacting particles of the feedstock containing particulate carbon and a surface, such as the inner surface of a deagglomeration conduit.

[00186] The feedstock containing deagglomerated particulate carbon (or the carrier gas that composes it) can be injected into the reactor at a pressure of 0.5 bar to 2 bar, preferably 0.7 bar to 1.5 bar, more preferably 0.8 to 1.3 bar, and even more preferably 0.8 to 1.2 bar. As mentioned earlier, the pressure must be adjusted according to the injection position of the feedstock. For example, the pressure in a combustion chamber is higher than the pressure at the choke point, so the feedstock containing deagglomerated particulate carbon or the carrier gas that composes it must be injected at higher pressures into the combustion chamber.

[00187] , and the carrier gas also includes H2O and / or additives. Water (H2O) can prevent the reagglomeration of particles in the carrier gas. Therefore, the feedstock containing deagglomerated carbon particles must be complemented by a carrier gas, and the carrier gas may further comprise H2O in an amount of 1 to 10% by volume, preferably 2 to 8% by volume, more preferably Petition 870250076402, dated 08 / 28 / 2025, page 53 / 136 46 / 106 from 3 to 7% by volume, based on the total volume of the carrier gas that makes up the feedstock containing deagglomerated carbon particles.

[00188] Raw material containing particulate carbon and / or raw material containing deagglomerated carbon is generally composed of a carrier gas.

[00189] Deagglomeration may be carried out in a particle feed and mixing device in a reactor comprising: (i) a carrier gas passage extending through said feed and mixing device, (ii) at least one carrier gas inlet, which is in fluidic communication with said carrier gas passage, (iii) at least one particle inlet, (iv) a mixing chamber that is in fluidic communication with said at least one particle inlet and with said carrier gas inlet, (v) a deagglomeration conduit that is in fluidic communication with said mixing chamber, (vi) at least one outlet for said carrier gas that carries particles that have been fed into said mixing chamber, wherein said at least one outlet is in fluidic communication with said deagglomeration conduit,and (vii) means for accelerating and injecting a carrier gas flow into said mixing chamber.

[00190] The said gas passage must extend along a longitudinal axis through the said feeding and mixing device and, preferably, at least one inlet, the said mixing chamber, the said deagglomeration conduit and the said outlet are aligned with the said longitudinal axis.

[00191] The said particle inlet must be configured to feed particles into the said mixing chamber at an angle relative to a carrier gas jet discharged into the said chamber. Petition 870250076402, dated 08 / 28 / 2025, p. 54 / 136 47 / 106 mixing jet, preferably perpendicular to the carrier gas jet. However, the angle is not particularly limited for the present invention.

[00192] The aforementioned means for accelerating and injecting the carrier gas flow may include at least one jet nozzle (nozzle). The jet nozzle is configured to accelerate the carrier gas flow. This means that the nozzle (or jet nozzle) is positioned so that the nozzle converges in one flow direction, so that the gas flow is accelerated after exiting the nozzle and entering the mixing chamber. In other words, the aforementioned means for accelerating and injecting the aforementioned carrier gas flow is preferably convergent in one flow direction extending from the aforementioned at least one carrier gas inlet towards the aforementioned at least one outlet.

[00193] The jet nozzle in question may be a Laval nozzle. Such a Laval nozzle (or nozzle) may comprise (in the following order) a converging section, a throat, and a diverging section. Typically, the converging section reduces the nozzle diameter so that the gas flow is accelerated. The diverging section increases the diameter in this section. However, the diameter increased by the diverging section is still smaller than the diameter before the converging section. Consequently, a nozzle comprising in the following order a converging section, a throat, and a diverging section accelerates the gas flow.

[00194] The cross-sectional area is generally circular or elliptical at each point of the jet nozzle.

[00195] The said jet nozzle may comprise a divergent section and the angle of the divergent section may be from 2 to 30°, preferably from 3 to 20°, more preferably from 4 to 15° and most preferably from 5 to 10°.

[00196] The jet nozzle may comprise a converging section and the maximum internal diameter of the converging section may be from 5 to 50 Petition 870250076402, dated 08 / 28 / 2025, page 55 / 136 48 / 106 mm, preferably 8 to 40 mm, more preferably 10 to 30 mm, and most preferably 12 to 20 mm.

[00197] The minimum internal diameter of the convergent section, divergent section and / or the internal diameter of the throat may be from 0.6 to 30 mm, preferably from 1.2 to 18 mm, more preferably from 1.9 to 12 mm and most preferably from 3 to 9 mm.

[00198] The minimum internal diameter of the convergent section, the divergent section, and the internal diameter of the throat must be the same. In other words, the convergent, throat, and divergent sections are generally directly connected to each other.

[00199] The jet nozzle may comprise a divergent section and the maximum internal diameter of the divergent section may be from 0.3 to 11 mm, preferably from 0.5 to 7 mm, more preferably from 0.9 to 5 mm and most preferably from 1.1 to 4 mm.

[00200] The minimum internal diameter of the converging section must be greater than the maximum internal diameter of the converging section, preferably the difference between the maximum internal diameters of the converging and diverging sections is 5 to 30 mm, preferably 8 to 20 mm, more preferably 9 to 18 mm and most preferably 10 to 15 mm.

[00201] The maximum internal diameter of the converging section may be greater than the maximum internal diameter of the diverging section.

[00202] The distance between the acceleration and injection medium and the constant internal diameter duct can be from 2 to 20 mm, preferably from 2.5 to 15 mm, more preferably from 3 to 10 mm, and even more preferably from 3.5 to 7 mm. A specific distance between the aforementioned components improves particle deagglomeration, since the jet stream flows directly to the deagglomeration duct. In this way, turbulence can be avoided and the loss of jet stream velocity is minimized. Petition 870250076402, dated 08 / 28 / 2025, page 56 / 136 49 / 106

[00203] It is possible that the means for accelerating and injecting the carrier gas (or nozzle) is positioned in such a way that the means for accelerating and injecting the carrier gas projects into the cavity of the inlet funnel of the deagglomeration conduit.

[00204] The aforementioned deagglomeration conduit typically comprises a conduit with a constant internal diameter. In said conduit with a constant internal diameter, the particles collide with each other or with the wall of the conduit with a constant internal diameter to further deagglomerate. Said deagglomeration conduit may be configured as a diffuser.

[00205] The deagglomeration conduit may comprise, from downstream to upstream, an inlet funnel, a conduit with a constant internal diameter, and a diffuser nozzle that diverges in the said flow direction. The divergence nozzle must continuously increase the internal diameter of the deagglomeration conduit. In this way, the flow of the carrier gas is not interrupted and turbulence is avoided. The angle of said diffuser nozzle may be from 1 to 30°, preferably from 2 to 20°, more preferably from 3 to 15°, and most preferably from 4 to 8°. The angle of said inlet funnel may be from 20 to 80°, preferably from 30 to 75°, more preferably from 40 to 70°, and most preferably from 50 to 65°.

[00206] The longitudinal axis of said deagglomeration conduit may be coaxial to the longitudinal axis of the feeding and mixing device. The coaxial arrangement improves overall acceleration as well as deagglomeration.

[00207] The internal diameter of the conduit with constant internal diameter can be from 1 to 20 mm, preferably from 2 to 10 mm, more preferably from 3 to 7 mm and, even more preferably, from 4 to 6 mm. The internal diameter can influence deagglomeration. Consequently, the diameter must be selected for the raw material. Petition 870250076402, dated 08 / 28 / 2025, page 57 / 136 50 / 106 specific to particles and, preferably, for mass flow.

[00208] The maximum internal diameter of the diffuser nozzle is greater than the internal diameter of the conduit, which has a constant internal diameter. The maximum internal diameter of the diffuser nozzle should be between 5 and 50 mm, preferably between 8 and 40 mm, more preferably between 10 and 30 mm, and even more preferably between 12 and 20 mm.

[00209] The diffuser nozzle and the converging section of the jet nozzle may have the same maximum internal diameter.

[00210] The maximum internal diameter of said diffuser nozzle may be from 5 to 50 mm, preferably from 8 to 40 mm, more preferably from 10 to 30 mm and even more preferably from 12 to 20 mm.

[00211] The length of the conduit with constant internal diameter may vary between 3 and 500 mm, preferably from 5 to 200 mm, more preferably from 10 to 50 mm and, even more preferably, from 13 to 30 mm. The length of said conduit may have a beneficial influence on the deagglomeration of particles (raw material containing carbon particles). A longer conduit generally results in better deagglomeration.

[00212] The length of the diffuser nozzle can be between 10 and 300 mm, preferably 20 to 200 mm, more preferably 25 to 150 mm and most preferably 30 to 100 mm.

[00213] The internal diameter of the conduit with constant internal diameter must be greater than the maximum internal diameter of the medium outlet in order to accelerate and inject a flow of the carrier gas.

[00214] The means for accelerating and injecting a carrier gas flow, the mixing chamber and the deagglomeration duct must be configured so that the carrier gas jet is discharged into the deagglomeration duct.

[00215] The feeding and mixing device may further comprise at least one hopper upstream of the said at least Petition 870250076402, dated 08 / 28 / 2025, page 58 / 136 51 / 106 one particle entry.

[00216] At least one screw conveyor, such as a screw conveyor, is frequently present upstream of said at least one particle inlet. The screw conveyor must be configured to supply a constant quantity of particles (or feedstock containing carbon particles) to the mixing chamber. Consequently, the supply of particles can be controlled by the screw conveyor.

[00217] The particles mentioned for the feeding and mixing device are the raw material containing particulate carbon and the reactor is typically an entrained flow reactor for the manufacture of carbon black.

[00218] The feed and mixing often further comprise a pressure tank for the particles, wherein the pressure tank is in fluid communication with said at least one particle inlet and, optionally, with said at least one screw conveyor. Preferably, there are two pressure tanks, a first pressure tank being connected to a second pressure tank. Both pressure tanks may be connected by means of a valve.

[00219] A reactor system may be provided comprising a entrained flow reactor and a feed and mixing device, wherein said feed and mixing device is in fluid communication with said reactor. Said feed and mixing device shall be connected to a plurality of inlets of said reactor, preferably by injection lances.

[00220] The aforementioned feeding and mixing device may be in fluid connection with a choke, a combustion chamber and / or a tunnel upstream of a quenching area of ​​a entrained flow reactor. The said reactor may be an entrained flow reactor. Petition 870250076402, dated 08 / 28 / 2025, page 59 / 136 52 / 106 of, preferably a furnace reactor.

[00221] A method can be provided for injecting particulate material into a reactor comprising the steps of (a) deagglomerating and entraining particles in a carrier gas stream, preferably using a feeding and mixing device, (b) injecting the carrier gas stream comprising deagglomerated particles obtained in step (a) into said reactor.

[00222] The method may be a method for the manufacture of carbon black and the particulate material is a feedstock containing particulate carbon and the reactor is an entrained flow reactor for the manufacture of carbon black, preferably a furnace reactor.

[00223] The said raw material containing particulate carbon can be injected into the said entrained flow reactor by a plurality of inlets, preferably by a plurality of injection lances.

[00224] The carrier gas flow can be accelerated and flows through a mixing chamber to a deagglomeration conduit.

[00225] Deagglomeration can be achieved by accelerating the particles in a carrier gas stream and colliding the particles with the inner surface of a deagglomeration conduit.

[00226] The carrier gas is generally accelerated to more than 1 Ma, preferably from 1.01 Ma to 1.7 Ma, more preferably from 1.1 Ma to 1.6 Ma and most preferably from 1.2 Ma to 1.5 Ma.

[00227] The particles can be subjected to the carrier gas jet, perpendicular to the carrier gas jet.

[00228] The carrier gas stream containing deagglomerated particles can be injected into the reactor at a pressure of 0.5 bar to 2 bar, preferably 0.7 bar to 1.5 bar, more preferably 0.8 to 1.3 bar and even more preferably 0.8 to 1.2 bar.

[00229] The carrier gas may also contain H2O and / or additives. The Petition 870250076402, dated 08 / 28 / 2025, p. 60 / 136 53 / 106 Carrier gas may contain H2O in an amount of 1 to 10% by volume. H2O may prevent the reagglomeration of particles.

[00230] The feeding and mixing device can be used to deagglomerate particles, preferably a raw material containing particulate carbon.

[00231] In addition, carbon black produced according to the inventive method is provided. Said carbon black may comprise new carbon black as well as recovered carbon black.

[00232] Carbon blacks are included in many polymeric compositions, for example, to modify their color and mechanical, electrical and / or processing properties. Carbon blacks are commonly added, for example, to rubber compositions used in the manufacture of tires or their components to impart electrically dissipative properties to the insulating matrix. At the same time, carbon black additives affect mechanical and elastic properties, such as stiffness, abrasion resistance and hysteresis, which greatly affect the performance of the resulting tire, for example, in terms of rolling resistance and durability.

[00233] According to the present invention, a composition comprising (A) an elastomeric polymeric material and (B) carbon black obtained according to the present invention is provided. It should be noted that the article provided, derived from said composition, can also be used as a raw material.

[00234] The term composition, as used herein, refers to a material composed of multiple chemical species or constituent components. An elastomeric polymeric material is understood to be a material consisting essentially of an elastomeric polymer. The term polymer is used herein in its common meaning in the art, referring to macromolecular compounds, i.e., compounds with a relatively high molecular mass (e.g., 500). Petition 870250076402, dated 08 / 28 / 2025, page 61 / 136 54 / 106 One or more), whose structure comprises multiple repeating units (also called mers) derived, actually or conceptually, from chemical species of relatively low molecular mass. The term elastomeric polymer is used here in its common meaning in the art, referring to a polymer that is elastic.

[00235] Particularly useful as elastomeric polymeric materials (or elastomeric polymeric material) for the practice of this invention are elastomers, such as rubber materials. The elastomeric polymeric material (A) of the composition according to the present invention may comprise one or more rubbers. The terms rubber, rubber material, and elastomer may be used interchangeably throughout this description unless otherwise indicated. Rubbers that may be used according to the present invention include those containing olefinic unsaturation, i.e., diene-based rubber materials, as well as non-diene-based rubber materials. The term diene-based rubber materials is intended to include natural and synthetic rubbers or mixtures thereof. The elastomeric polymeric material (a) may consist of synthetic rubber.

[00236] The elastomeric polymeric material (A) of the composition according to the present invention may comprise natural and / or synthetic rubber.

[00237] Natural rubber can be used in its raw form and in various processed forms conventionally known in the rubber processing area. Natural rubber can, for example, be obtained from rubber trees (Helvea brasiliensis), guayule and dandelion. Consequently, the elastomeric polymeric material (a) may comprise or consist of natural rubber.

[00238] Synthetic rubber may comprise styrene-butadiene rubber, such as styrene-butadiene emulsion rubber Petition 870250076402, dated 08 / 28 / 2025, page 62 / 136 55 / 106 (ESBR) and styrene-butadiene solution rubber (SSBR), polybutadiene, polyisoprene, ethylene-propylene-diene rubber (EPDM), ethylene-propylene rubber (EPM), butyl rubber, halogenated butyl rubber, chlorinated polyethylene, chlorosulfonated polyethylene, acrylonitrile-butadiene rubber, hydrogenated acrylonitrile-butadiene rubber, polychloroprene, acrylate rubber, ethylene vinyl acetate rubber, ethylene-acrylic rubber, epichlorohydrin rubber, silicone rubber, fluorosilicone rubber, fluorocarbon rubber, or a mixture of combinations of any of the foregoing. According to the invention, synthetic rubber can also be obtained from a renewable source material. For example, polybutadiene can be produced from alcohol obtained by fermentation of plant biomass.

[00239] Suitable rubbers may also include functionalized rubbers and rubbers coupled with silicon or tin. For example, rubbers may be functionalized with functional groups such as amine, alkoxy, silyl, thiols, thioesters, thioether, sulfanil, mercapto, sulfide, or combinations thereof. One or more functionalities may be primary, secondary, or tertiary and may be located at one or both ends of the chain (e.g., α,ω functionalization), pendant from the polymer backbone, and / or arranged within the polymer backbone. The rubber according to the invention may also be partially crosslinked. Thus, prior to use in the composition of the present invention, part of the polymer chains of the rubber material may be crosslinked by means of a coupling agent or without it.

[00240] The composition according to the invention may, in particular, be a curable composition, such as, for example, a vulcanizable rubber composition. The term vulcanizable rubber composition refers to a composition of a rubber component, Petition 870250076402, dated 08 / 28 / 2025, p. 63 / 136 56 / 106 optionally with various other ingredients conventionally used in the rubber compounding technique, which can be cured by vulcanization under the formation of a vulcanizate. The terms curable and vulcanizable are used interchangeably throughout this description unless otherwise indicated, and refer to a chemical reaction that links polymer chains together by means of a crosslinker or vulcanizing agent. The curing reaction can be induced by any means known in the art, such as light, moisture, heat and / or the addition of a crosslinker.

[00241] The elastomeric polymeric material (A), according to the invention, may comprise natural rubber. According to the invention, the natural rubber may comprise natural rubber obtained from rubber trees (Helvea brasiliensis), guayule, dandelion, or mixtures of combinations of any of the foregoing. The natural rubber may comprise natural rubber obtained from guayule and / or dandelion. The elastomeric polymeric material (A) may comprise 5 phr or more of natural rubber, such as 10 phr or more, or 15 phr or more, or 20 phr or more, or 30 phr or more, or 40 phr or more, or 50 phr or more, or 60 phr or more, or 70 phr or more, or 80 phr or more. As used herein, the term phr refers to parts by weight of the respective material per 100 parts by weight of rubber or elastomer.The elastomeric polymeric material (A) may contain 100 phr or less of natural rubber, such as 95 phr or less, or 90 phr or less, or 85 phr or less, or 80 phr or less, or 75 phr or less, or 70 phr or less, or 65 phr or less, or 60 phr or less. The elastomeric polymeric material (A) may contain natural rubber in a range between any of the lower and upper limits mentioned. For example, the elastomeric polymeric material (A) may contain natural rubber in a range of 5 to 95 phr, such as in a range of 10 to 90 phr, or in a range of 20 to 80 phr, or in a range of 30 to 70 phr. Petition 870250076402, dated 08 / 28 / 2025, p. 64 / 136 57 / 106 or in a range of 40 to 60 phr. According to the present invention, the elastomeric polymeric material (A) may consist of natural rubber.

[00242] The elastomeric polymeric material (A) according to the invention may comprise a synthetic rubber. According to the invention, the synthetic rubber may comprise synthetic rubber obtained from a renewable source material. The renewable source material according to the present invention may be alcohol obtained by fermentation of plant biomass. For example, the synthetic rubber may comprise polybutadiene obtained from alcohol obtained by fermentation of plant biomass. The elastomeric polymeric material (A) may comprise 5 phr or more of synthetic rubber, such as 10 phr or more, or 15 phr or more, or 20 phr or more, or 30 phr or more, or 40 phr or more, or 50 phr or more, or 60 phr or more, or 70 phr or more, or 80 phr or more. As used herein, the term phr refers to parts by weight of the respective material per 100 parts by weight of rubber or elastomer.The elastomeric polymeric material (A) may comprise 100 phr or less of synthetic rubber, such as 95 phr or less, or 90 phr or less, or 85 phr or less, or 80 phr or less, or 75 phr or less, or 70 phr or less, or 65 phr or less, or 60 phr or less. The elastomeric polymeric material (A) may comprise synthetic rubber in a range between any of the aforementioned lower and upper limits. For example, the elastomeric polymeric material (A) may comprise synthetic rubber in a range of 5 to 95 phr, such as in a range of 10 to 90 phr, or in a range of 20 to 80 phr, or in a range of 30 to 70 phr, or in a range of 40 to 60 phr. According to the present invention, the elastomeric polymeric material (A) may consist of synthetic rubber.

[00243] According to the present invention, the elastomeric polymeric material (A) may comprise a mixture of natural rubber and Petition 870250076402, dated 08 / 28 / 2025, page 65 / 136 58 / 106 synthetic rubber. The elastomeric polymeric material (A) may comprise 5 to 100 phr of natural rubber and 5 to 100 phr of synthetic rubber, such as 10 to 90 phr of natural rubber and 10 to 90 phr of synthetic rubber, or 20 to 80 phr of natural rubber and 20 to 80 phr of synthetic rubber, or 30 to 70 phr of natural rubber and 30 to 70 phr of synthetic rubber, or 40 to 60 phr of natural rubber and 40 to 60 phr of synthetic rubber, or 40 to 100 phr of natural rubber and 5 to 60 phr of synthetic rubber, or 50 to 95 phr of natural rubber and 5 to 50 phr of synthetic rubber, or 60 to 90 phr of natural rubber and 10 to 50 phr of synthetic rubber, or 5 to 40 phr of natural rubber and 60 to 100 phr of synthetic rubber, or 10 to 20 phr of natural rubber and 80 to 90 phr.For example, the elastomeric polymeric material (A) may comprise 50 phr of natural rubber and 50 phr of synthetic rubber, or the elastomeric polymeric material (A) may comprise 5 phr of natural rubber and 95 phr of synthetic rubber.

[00244] The synthetic rubber according to the present invention preferably comprises styrene-butadiene emulsion rubber (ESBR), polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a mixture of combinations of any of the foregoing, more preferably polyisoprene and / or polybutadiene, even more preferably polybutadiene. The synthetic rubber according to the present invention preferably consists of styrene-butadiene emulsion rubber (ESBR), polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a mixture of combinations of any of the foregoing, more preferably polyisoprene and / or polybutadiene, even more preferably polybutadiene. The synthetic rubber may comprise styrene-butadiene emulsion rubber (ESBR), polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a mixture of Petition 870250076402, dated 08 / 28 / 2025, page 66 / 136 59 / 106 combinations of any of the foregoing, preferably polyisoprene or polybutadiene, more preferably polybutadiene. Synthetic rubber may comprise or consist of polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a mixture of combinations of any of the foregoing, preferably polyisoprene or polybutadiene, more preferably polybutadiene. Synthetic rubber may comprise or consist of polybutadiene, polyisoprene, halogenated butyl rubber, or a mixture of combinations of any of the foregoing, preferably polyisoprene or polybutadiene, more preferably polybutadiene.

[00245] The carbon black produced may also be pulverized before being added to the composition. Thus, the composition may contain pulverized carbon black.

[00246] The composition may comprise from 3 to 200 phr of carbon black obtained according to the present invention (B), preferably from 5 to 190 phr of carbon black obtained according to the present invention (B), more preferably from 10 to 150 phr of carbon black obtained according to the present invention (B), even more preferably from 20 to 130 phr of carbon black obtained according to the present invention (B), most preferably from 30 to 100 phr of carbon black (B) obtained according to the present invention.

[00247] The composition may comprise one or more additives selected from among vulcanizing agents, curing aids such as primary and secondary vulcanization accelerators, pre-vulcanization activators and inhibitors, processing additives such as oils, waxes, resins, plasticizers, softeners, rheology modifiers, pigments, peptizing agents, coupling agents, surfactants, biocides and antidegradants such as heat or light stabilizers, antioxidants and antiozonates, metal oxides, metal hydroxides and filler materials such as silica, organosilica, nanotubes of Petition 870250076402, dated 08 / 28 / 2025, page 67 / 136 60 / 106 carbon, carbon fibers, graphite and metallic fibers.

[00248] The composition of the present invention can be obtained and processed by common elastomer processing technology. The composition according to the present invention can, for example, be obtained by combining the carbon black (B) of the present invention and any optional ingredients, if used, with the elastomeric polymeric material (A) and mixing it, for example, to disperse the carbon black (B) and any optional ingredients, if used, in the elastomeric polymeric material (A). The dispersion can be obtained by any means known in the art, such as mixing, stirring, grinding, kneading, ultrasound, a dissolver, a mixer-shaker, rotor-stator dispersion sets or high-pressure homogenizers, or a combination thereof. For example, a laboratory mixer with an interlaced rotor geometry can be used.The dispersion can, for example, be carried out until the carbon black (B) is homogeneously dispersed in the elastomeric polymeric material (A), resulting in a dispersion index greater than or higher than 95%, preferably 97% or higher, or more than 99% according to the classification as per ASTM D2663-88, test method B.

[00249] The preparation of the composition according to the present invention can, for example, be carried out in a multi-step process: initially, carbon black (B) and, optionally, non-curing additives, if used, can be added to the elastomeric polymeric material (A) concomitantly or successively. The elastomeric polymeric material (A), the carbon black (B) and the additives, if used, can then be mixed, typically at a temperature in the range of 40°C to 160°C, for a total mixing time of less than 10 minutes, such as, for example, in the range of 2 to 8 minutes. Subsequently, the mixture obtained can be combined with one or more additives. Petition 870250076402, dated 08 / 28 / 2025, p. 68 / 136 61 / 106 healing applications for less than 5 minutes, typically less than 3 minutes, preferably for about 2.5 minutes, at a temperature below 115°C.

[00250] The process may include additional steps such as extrusion or cooling of the product to ambient temperature and storage for further processing. The process may also include a curing step, which may be carried out, for example, by subjecting the composition to thermal curing conditions, for example, at a temperature of 120-200°C for a period of 5 minutes to 3 hours. Curing may, for example, be carried out in a curing press, for example, at a temperature of 140-180°C for 5 to 60 minutes at a pressure between 100 and 150 bar.

[00251] As can be seen, the compositions according to the invention can be used in various technical applications requiring carbon black-filled polymer-based materials, for example, to impart antistatic or electrically conductive properties, color, mechanical reinforcement and / or low hysteresis properties. Mechanical properties of interest, particularly for tire production, include tear resistance, rebound and hysteresis. The compositions according to the present invention provide cured compositions that exhibit good and beneficial mechanical properties, especially for tire production. Beneficial mechanical properties according to the present invention are, for example, high tensile strength, high rebound and low hysteresis. The composition according to the present invention provides cured compositions with mechanical properties comparable to rubber compositions comprising conventional carbon blacks.

[00252] Consequently, the invention also relates to articles, and particularly to tires, made of or comprising the composition mentioned above, according to the invention. The tire, according Petition 870250076402, dated 08 / 28 / 2025, page 69 / 136 62 / 106 with the present invention, may comprise a tread, carcass, sidewall, inner lining, apex, shoulder, impact protection strip, bead lining and / or filling, wherein at least one of the foregoing is made of or comprises a composition according to the invention. Such tires include, for example, but not limited to, truck tires, passenger tires, off-road tires, aircraft tires, agricultural tires and excavator tires. The tires and / or tire components described may also be used as rubber granules.

[00253] The tire may comprise a sidewall, wherein the sidewall is made of the composition according to the invention, wherein the composition preferably comprises: (A) 40 to 60 phr of natural rubber and 40 to 60 phr of synthetic rubber, preferably 50 to 60 phr of natural rubber and 40 to 50 phr of synthetic rubber, more preferably 55 phr of natural rubber and 45 phr of synthetic rubber, wherein the synthetic rubber preferably comprises polybutadiene, more preferably consists of polybutadiene; and (B) 30 to 70 phr of carbon black, preferably 40 to 60 phr of carbon black.

[00254] The tire may comprise a carcass, wherein the carcass is made of the composition according to the invention, wherein the composition preferably comprises: (A) 40 to 80 phr of natural rubber and 20 to 60 phr of synthetic rubber, preferably 50 to 70 phr of natural rubber and 30 to 50 phr of synthetic rubber, more preferably 60 phr of natural rubber and 40 phr of synthetic rubber, wherein the synthetic rubber preferably comprises polybutadiene and styrene-butadiene emulsion rubber (ESBR), more preferably comprising 20 phr of polybutadiene and 20 phr of styrene-butadiene emulsion rubber (ESBR); and (B) 5 to 70 phr of carbon black, preferably 40 to 60 phr of carbon black. Petition 870250076402, dated 08 / 28 / 2025, p. 70 / 136 63 / 106 grains of tobacco, more preferably 50 phr of carbon black.

[00255] The tire comprises a liner, wherein the liner is made of the composition according to the invention, wherein the composition preferably comprises: (A) 30 to 70 phr of natural rubber and 30 to 70 phr of synthetic rubber, preferably 40 to 60 phr of natural rubber and 40 to 60 phr of synthetic rubber, more preferably 50 phr of natural rubber and 50 phr of synthetic rubber, wherein the synthetic rubber preferably comprises styrene-butadiene emulsion rubber (ESBR), more preferably consists of styrene-butadiene emulsion rubber (ESBR); and (B) 55 to 95 phr of carbon black, preferably 65 to 85 phr of carbon black, preferably 75 phr of carbon black.

[00256] The tire may comprise a bead and / or apex filler, wherein the bead and / or apex filler is / are made of the composition according to the invention, wherein the composition preferably comprises: (A) 80 to 100 phr of natural rubber, preferably 90 to 100 phr of natural rubber, more preferably 100 phr of natural rubber; and (B) 35 to 75 phr of carbon black, preferably 45 to 65 phr of carbon black, more preferably 55 phr of carbon black.

[00257] The tire may comprise an inner lining, wherein the inner lining is made of the composition according to the invention, wherein the composition preferably comprises (A) 80 to 100 phr of synthetic rubber, preferably 90 to 100 phr of synthetic rubber, more preferably 100 phr of synthetic rubber, wherein the synthetic rubber preferably comprises a halogenated butyl rubber, more preferably consists of a halogenated butyl rubber; and (B) 40 to 80 phr of carbon black, preferably 50 to 70 phr of carbon black, more preferably 60 phr of carbon black. Petition 870250076402, dated 08 / 28 / 2025, page 71 / 136 64 / 106

[00258] The tire may comprise a tread, preferably a truck tire, wherein the tread is made of the composition according to the invention, wherein the composition preferably comprises (A) 60 to 95 phr of natural rubber and 5 to 40 phr of synthetic rubber, preferably 70 to 85 phr of natural rubber and 15 to 30 phr of synthetic rubber, more preferably 80 phr of natural rubber and 20 phr of synthetic rubber, wherein the synthetic rubber preferably comprises polybutadiene, more preferably consists of polybutadiene; and (B) 30 to 70 phr of carbon black, preferably 40 to 60 phr of carbon black, more preferably 50 phr of carbon black.

[00259] The tire may comprise a tread, preferably a passenger car tire, wherein the tread is made of the composition according to the invention, wherein the composition preferably comprises (A) 80 to 100 phr of synthetic rubber, preferably 90 to 100 phr of synthetic rubber, more preferably 100 phr of synthetic rubber, wherein the synthetic rubber preferably comprises solution styrene-butadiene rubber (SSBR) and polybutadiene, more preferably comprises 70 phr of solution styrene-butadiene rubber (SSBR) and 30 phr of polybutadiene; and (B) 35 to 75 phr of carbon black, preferably 45 to 65 phr of carbon black, more preferably 55 phr of carbon black.

[00260] The tire may comprise a tread, preferably a passenger car tire, wherein the tread is made of the composition according to the invention, wherein the composition preferably comprises (A) 80 to 100 phr of synthetic rubber, preferably 90 to 100 phr of synthetic rubber, more preferably 100 phr of synthetic rubber, wherein the synthetic rubber preferably comprises styrene rubber. Petition 870250076402, dated 08 / 28 / 2025, p. 72 / 136 65 / 106 butadiene in solution (SSBR) and polybutadiene, more preferably comprising 70 phr of styrene-butadiene rubber in solution (SSBR) and 30 phr of polybutadiene; and (B) 3 to 25 phr of carbon black, preferably 5 to 15 phr of carbon black, more preferably 5 phr of carbon black; and (C) 60 to 100 phr of silica, preferably 70 to 90 phr of silica, more preferably 80 phr of silica.

[00261] The tire may comprise a tread, preferably an off-road (OTR) tire, wherein the tread is made of the composition according to the invention, wherein the composition preferably comprises (A) 80 to 100 phr of natural rubber, preferably 90 to 100 phr of natural rubber, more preferably 100 phr of natural rubber; and (B) 35 to 75 phr of carbon black, preferably 45 to 75 phr of carbon black, more preferably 55 phr of carbon black.

[00262] The article may be a cable sheath, tube, transmission belt, conveyor belt, roller coating, shoe sole, hose, sealing element, profile, damping element, coating or colored or printed article.

[00263] In addition, the article may be a conveyor belt, wherein the conveyor belt is made of the composition according to the invention, wherein the composition preferably comprises (A) 60 to 95 phr of natural rubber and 5 to 40 phr of synthetic rubber, preferably 70 to 85 phr of natural rubber and 15 to 30 phr of synthetic rubber, more preferably 80 phr of natural rubber and 20 phr of synthetic rubber, wherein the synthetic rubber preferably comprises polybutadiene, more preferably consists of polybutadiene; and (B) 30 to 70 phr of carbon black, preferably 40 to 60 phr of carbon black, more preferably Petition 870250076402, dated 08 / 28 / 2025, p. 73 / 136 66 / 106 mind of 50 phr carbon black.

[00264] In addition, the present invention relates to the use of the aforementioned composition according to the present invention to produce a tire, preferably a pneumatic tire, a tire tread, a belt, a belt reinforcement, a carcass, a carcass reinforcement, a sidewall, inner lining, apex, shoulder, protective strip, lining, bead filler, a cord sheath, a tube, a transmission belt, a conveyor belt, a roller cover, a shoe sole, a hose, a sealing element, a profile, a damping element, a coating or a colored or printed article.

[00265] In addition, the present invention utilizes raw material containing deagglomerated particulate carbon for the manufacture of carbon black in an entrained flow reactor.

[00266] The invention will now be described with reference to the accompanying figures, which do not limit the scope and extent of the invention. The description provided is merely exemplary and illustrative. However, specific features exemplified in the figures can be used to further restrict the scope of the invention and the claims.

[00267] Figure 1 shows a furnace reactor 100 comprising a combustion chamber 101, a choke 102, and a tunnel 103. The reactor has an inner lining 106 as well as an outer lining 105. The combustion chamber 101 comprises means for injecting fuel 101b and oxygen-containing gas 101a. In the figure, the oxygen-containing gas is injected into the combustion chamber 101 tangentially or radially by means of an oxygen-containing gas 101a, and the fuel is injected into the combustion chamber 101 axially by means of a fuel injection device 101b. It is preferable that the oxygen-containing gas be preheated to Petition 870250076402, dated 08 / 28 / 2025, page 74 / 136 67 / 106 a temperature described in the description. It is possible to adjust the temperature of the hot gas flow by preheating the oxygen-containing gas. Alternatively, the fuel can be preheated. In combustion chamber 101, the fuel is burned in the presence of oxygen-containing gas. After combustion, the temperature of the hot carrier gas is above 800°C to bring the particulate carbon-containing feedstock to the temperature required for pyrolysis. The particulate carbon-containing feedstock can be injected directly into combustion chamber 101, at the choke point 102, or into tunnel 103. The particulate carbon-containing feedstock can also be injected in any of the aforementioned combinations, either at choke point 102 or into tunnel 103. The furnace reactor 100 comprises multiple positions for quenching (104a, 104b, 104c, 104d).The quenching medium, usually water, reduces the temperature of the hot gas stream (or product mixture), so that the carbon black formation reaction is stopped. Consequently, the position of the rapid cooling influences the residence time of the feedstock as well as the components derived from the feedstock. This means that the residence time increases if the position of the rapid cooling is set further downstream in the reactor. For example, rapid cooling at a position 104a) near the choke point 102 results in a low residence time, and rapid cooling at a position 104c) downstream in the reactor results in a high residence time. The reaction volume is the volume of the reactor between the feedstock injection and the position of the rapid cooling.If the raw material is injected into tunnel 103 and the distance between the rapid cooling position and the raw material injection point is 4200 mm, and the tunnel diameter is 200 m, the resulting reaction volume will be 132 L. The feed flow rate of the raw material containing particulate carbon should be adjusted accordingly. Petition 870250076402, dated 08 / 28 / 2025, page 75 / 136 68 / 106 of the reaction volume, as mentioned in the description. For the present invention, a quenching position at the rear of the tunnel is particularly preferred so that the particulate carbon-containing feedstock has sufficient time for evaporation or pyrolysis.

[00268] Referring to Figure 2, a feeding and mixing device 200 is shown comprising a carrier gas inlet 204, a particle inlet 201, means for accelerating and injecting a carrier gas stream 207, a deagglomeration conduit 209, a mixing chamber 206 and an outlet for the carrier gas particles (210). The carrier gas passage (212) is also indicated in Figure 2. The carrier gas passage (212) extends along a longitudinal axis through the feeding and mixing device. The carrier gas 203 enters the feed and mixing device 200 through the carrier gas inlet 204 and is accelerated in the means for accelerating and injecting a carrier gas stream 207. In Figure 2, the means for accelerating and injecting a carrier gas stream 207 are configured as a Laval nozzle. The Laval nozzle comprises a convergent area 207a) in the flow direction.The resulting carrier gas jet is injected into the mixing chamber 206. Particles, such as the carbon-containing feedstock 202, are injected perpendicularly into the mixing chamber 206. Consequently, the particles are carried into the accelerated carrier gas. The abrupt acceleration of the particles results in their deagglomeration. The accelerated carrier gas, composed of the particles, is subsequently injected into the deagglomeration conduit 209. In the deagglomeration conduit 209, the particles collide with each other or with the inner wall or inner surface of the deagglomeration conduit 209, thus achieving further deagglomeration. It is desirable that the means for accelerating and injecting a carrier gas stream 207 be configured so that the carrier gas jet is injected. Petition 870250076402, dated 08 / 28 / 2025, page 76 / 136 69 / 106 directly into the deagglomeration conduit 209. In this way, velocity loss can be minimized. The deagglomeration conduit 209 typically comprises, from downstream to upstream (in the flow direction), an inlet funnel 209a, a conduit with constant internal diameter 209b, and a diffuser nozzle diverging in the flow direction 209c. The inlet funnel 209a also allows for ideal flow behavior in the conduit with constant internal diameter 209b. The diffuser nozzle diverging in the flow direction 209c is also beneficial for flow behavior. The outlet 406 can be connected to the media for injecting the raw material into a reactor, as shown in Figure 1. It is preferable that a feeding and mixing device 200 supplies the deagglomerated raw material to multiple media for injection into the reactor. It is also desirable that the feeding and mixing device 200 comprise a screw conveyor connected to the particle inlet 201.The screw conveyor can supply a suitable quantity or weight of particles to the mixing chamber 206. Furthermore, the feeding and mixing device 200 can be operated under a pressure of 1.5 bar or 2 bar. A pressure tank for the particles (e.g., raw material containing carbon particles) can be installed. Such a pressure tank is in fluid connection with the particle inlet 201 and preferably connected to the feeding and mixing device 200 by means of a valve. Preferably, two pressure tanks are present, with a first pressure tank connected to a second pressure tank. Both pressure tanks can be connected by means of a valve.

[00269] Figure 3 shows a Laval 300 nozzle for use in the feeding and mixing device 200. The carrier gas passage 306 extends along a longitudinal axis through the Laval 300 nozzle. The carrier gas 304 enters the Laval 300 nozzle and is accelerated. Petition 870250076402, dated 08 / 28 / 2025, page 77 / 136 70 / 106 The carrier gas jet 305 then exits the Laval nozzle 300. The Laval nozzle 300 comprises a constant diameter section 301, a converging section 302a in the flow direction 302, a throat 303a and a diverging section 303. In the Laval nozzle 300, the carrier gas is accelerated to a velocity greater than 1 Ma.

[00270] Figure 4 shows the deagglomeration duct 400 for use in the feeding and mixing device 200. The carrier gas passage 407 extends along a longitudinal axis through the deagglomeration duct 400. The deagglomeration duct 400 comprises an inlet funnel 401, a duct with constant internal diameter 402, and a diffuser nozzle 403 diverging in the flow direction 403a. In addition, an outlet 404 is shown which can be connected to a device for injecting the deagglomerated particles (e.g., carbon-containing deagglomerated particles) 406 into the reactor.

[00271] In Figure 5, an alternative feeding and mixing device 500 is shown. The carrier gas passage 506 is also indicated in Figure 5. The carrier gas passage 506 extends along a longitudinal axis through said feeding and mixing device. Said feeding and mixing device 500 comprises an inlet 504 for the carrier gas 501, a mixing chamber 505, a particle inlet 502 and an outlet 503. A carrier gas 501 enters the feeding and mixing device 500. The carrier gas 501 must have a desirable velocity, such as below 1 m / s or between 2 m / s and 1 m / s or between 20 m / s and 200 m / s. Particles, such as particulate carbon-containing feedstock 202, are injected perpendicularly into the mixing chamber 507. Consequently, the particles will be carried into the accelerated carrier gas. The abrupt acceleration of the particles results in their deagglomeration. Outlet 503 can be connected to a reactor. Seme Petition 870250076402, dated 08 / 28 / 2025, p. 78 / 136 71 / 106 lhante ao aparelho de alimenta e mistura 200, um conveyivo de um elicoidal e pelo menos um tanque de pressão podem ser instalado.

[00272] In addition, the present invention will be described by means of the following aspects.

[00273] Aspect 1. A method for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, comprising: (a) provide a hot gas stream, (b) provide a feedstock containing particulate carbon, and (d) inject the particulate carbon contained in the hot gas stream to form carbon black, where the hot gas stream has a temperature of at least 800°C.

[00274] Aspect 2. The method, according to aspect 1, wherein step (b) further comprises the deagglomeration of particulate carbon containing and in step (d), the deagglomerated feedstock containing particulate carbon is injected into the hot gas stream to form carbon black.

[00275] Aspect 3. A method for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, comprising: (a) provide a stream of hot gas, (b) deagglomerate a feedstock containing carbon particles to provide a deagglomerated feedstock containing carbon particles, and (d) inject the deagglomerated feedstock containing carbon particles into the stream of hot gas to form carbon black, Petition 870250076402, dated 08 / 28 / 2025, page 79 / 136 72 / 106 where the hot gas stream has a temperature of at least 800°C.

[00276] Aspect 4. The method, according to any of the aspects above, in which the feedstock containing particulate carbon comprises inert compounds, coke, compounds containing C, H and / or carbon black, preferably ash and carbon black.

[00277] Aspect 5. The method, according to any of the aspects above, in which the feedstock containing particulate carbon further comprises inert compounds, in which the inert compounds comprise zinc, silicon, calcium, aluminum and / or iron.

[00278] Aspect 6. The method, according to any of the preceding aspects, wherein the feedstock containing particulate carbon comprises from 1 to 40% by weight of inert compounds, preferably from 3 to 30% by weight of inert compounds, more preferably from 4 to 20% by weight of inert compounds and, most preferably, from 5 to 15% by weight of inert compounds, based on the total weight of the feedstock containing particulate carbon.

[00279] Aspect 7. The method, according to any of the preceding aspects, wherein the feedstock containing particulate carbon further comprises carbon black, wherein the carbon black is present in the feedstock containing particulate carbon in an amount of 1 to 70% by weight, preferably 2 to 50% by weight, more preferably 5 to 40% by weight and even more preferably 10 to 30% by weight, based on the total weight of the feedstock containing particulate carbon.

[00280] Aspect 8. The method, according to any of the preceding aspects, wherein the raw material containing particulate carbon comprises from 10 to 100% by weight of compounds containing C,H, preferably from 20 to 99% by weight of compounds containing C,H, more preferably from 30 to 90% by weight of compounds containing Petition 870250076402, dated 08 / 28 / 2025, p. 80 / 136 73 / 106 containing C,H and, more preferably, 40 to 70% by weight of compounds containing C,H, based on the total weight of the raw material containing particulate carbon.

[00281] Aspect 9. The method, according to any of the preceding aspects, in which the raw material containing particulate carbon comprises rubber granules, plastic granules and / or biomass-based granules.

[00282] Aspect 10. The method, according to any of the preceding aspects, wherein the raw material containing particulate carbon comprises rubber granules, wherein the rubber granules comprise carbon black.

[00283] Aspect 11. The method, according to any of the preceding aspects, in which the raw material containing particulate carbon comprises agglomerated raw material.

[00284] Aspect 12. The method, according to any of the above aspects, wherein at least 50% by weight, preferably at least 60% by weight, more preferably at least 70% by weight, most preferably at least 80% by weight, of the feedstock containing particulate carbon has a particle size of 125 µm to 2 mm, preferably 125 µm to 1 mm, more preferably 250 µm to 1 mm and most preferably 500 µm to 1000 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00285] Aspect 13. The method, according to any of the preceding aspects, in which the particle size distribution of the feedstock containing particulate carbon is measured in accordance with ASTM D 1511-12 2017) and (a) Sieve No. 10 retains 1 to 10% by weight, preferably 1 to 8% by weight, more preferably 1 to 5% by weight and, even more preferably, 1 to 3% by weight of the feedstock. Petition 870250076402, dated 08 / 28 / 2025, p. 81 / 136 74 / 106 raw material containing carbon particles, and / or (b) Sieve No. 18 retains 1 to 25% by weight, preferably 2 to 20% by weight, more preferably 4 to 15% by weight, and even more preferably 5 to 12% by weight of the raw material containing carbon particles, and / or (c) Sieve No. 35 retains 10 to 80% by weight, preferably 15 to 70% by weight, more preferably 20 to 60% by weight, and even more preferably 25 to 55% by weight of the raw material containing carbon particles, and / or (d) Sieve No. 60 retains 5 to 70% by weight, preferably 10 to 60% by weight, more preferably 15 to 50% by weight, and even more preferably 20 to 45% by weight of the raw material containing carbon particles, and / or (e) Sieve No. 120 retains 1 to 80% by weight, preferably 7 to 70% by weight, more preferably 5 to 60% by weight and, even more preferably, 7 to 50% by weight of the raw material containing carbon particles,and / or (f) The lower receiving tray comprises less than 4% by weight, preferably less than 3% by weight, more preferably 0 to 2% by weight and even more preferably 0.01 to 1% by weight of the raw material containing particulate carbon.

[00286] Aspect 14. The method, according to any of the preceding aspects, wherein not more than 10% by weight, preferably not more than 5% by weight, more preferably not more than 4% by weight and more preferably not more than 2% by weight of the particulate carbon-containing feedstock has a particle size greater than 4 mm, preferably more than 2 mm, more preferably more than 1 mm and more preferably more than 0.5 mm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017). Petition 870250076402, dated 08 / 28 / 2025, p. 82 / 136 75 / 106

[00287] Aspect 15. The method, according to any of the preceding aspects, wherein not more than 10% by weight, preferably not more than 5% by weight, more preferably not more than 4% by weight and most preferably not more than 2% by weight of the particulate carbon-containing feedstock has a particle size less than 150 µm, preferably less than 125 µm, more preferably less than 110 µm and most preferably less than 100 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00288] Aspect 16. The method, according to any of the preceding aspects, wherein the cumulative particle size of 50% by weight of the feedstock containing particulate carbon is from 100 µm to 4 mm, preferably from 100 µm to 3 mm, more preferably from 100 µm to 2 mm and even more preferably from 100 µm to 500 µm, wherein the cumulative particle size of 50% by weight is measured in accordance with ASTM D 1511-12 2017).

[00289] Aspect 17. The method, according to any of the preceding aspects, wherein the weight average particle size Dw50 of the carbon-containing feedstock is from 100 µm to 4 mm, preferably 100 µm to 3 mm, more preferably 100 µm to 2 mm and even more preferably 100 µm to 500 µm, wherein the weight average particle size Dw50 is measured in accordance with ASTM D 1511-12 2017).

[00290] Aspect 18. The method, according to any of the preceding aspects, wherein the Dw10 particle size distribution of the carbon-containing feedstock is from 100 µm to 250 µm, preferably 110 µm to 220 µm, more preferably 120 µm to 210 µm and most preferably 130 µm to 200 µm, wherein the Dw10 particle size distribution is measured in accordance with ASTM D 1511-12 2017). Petition 870250076402, dated 08 / 28 / 2025, p. 83 / 136 76 / 106

[00291] Aspect 19. The method, according to any of the preceding aspects, wherein the particle size distribution of the Dw90 particulate carbon-containing feedstock is from 400 µm to 4 mm, preferably 500 µm to 3 mm, more preferably 600 µm to 2 mm and even more preferably 700 µm to 500 µm, wherein the Dw90 particle size distribution is measured in accordance with ASTM D 1511-12 2017).

[00292] Aspect 20. The method, according to any of the above aspects, wherein the range of particle size distributions of the particulate carbon-containing feedstock (Dw90Dw10) / Dw50 is from 0.2 to 1.8, preferably from 0.3 to 1.3, more preferably from 0.4 to 1.1, most preferably from 0.4 to 1.0, wherein the particle size distributions Dw10, Dw50 and Dw90 are measured in accordance with ASTM D 1511-12 2017).

[00293] Aspect 21. The method, according to any of the above aspects, in which the method for producing carbon black does not use liquid feedstock containing carbon for the production of carbon black.

[00294] Aspect 22. The method, according to any of the preceding aspects, in which the hot gas flow is obtained by electrical preheating, plasma heating and combustion of a fuel gas containing oxygen.

[00295] Aspect 23. The method, according to any of the preceding aspects, wherein the hot gas flow is provided by (a1) supplying fuel and oxygen-containing gas to a reactor combustion chamber, (b2) combustion of fuel in the combustion chamber to produce the hot gas flow.

[00296] Aspect 24. The method, according to any of the preceding aspects, in which the entrained flow reactor is a reactor of Petition 870250076402, dated 08 / 28 / 2025, p. 84 / 136 77 / 106 furnace.

[00297] Aspect 25. The method, according to any one of aspects 22 to 24, in which the feedstock containing particulate carbon is injected into the combustion chamber, into the choke and / or into the reactor tunnel of the furnace, preferably into the choke of the furnace reactor.

[00298] Aspect 26. The method, according to any of the above aspects, in which the hot gas stream has a temperature of 900 to 3500°C, preferably 950 to 3000°C, more preferably 1000 to 2000°C and, most preferably, 1200 to 1900°C.

[00299] Aspect 27. The method, according to any one of aspects 22 to 26, in which the oxygen-containing gas is preheated to a temperature between 200 and 1600°C, preferably 350 and 1400°C, more preferably 500 and 1200°C and most preferably 450 and 950°C.

[00300] Aspect 28. The method, according to any one of aspects 22 to 27, in which the fuel is preheated to a temperature between 50 and 750°C, preferably 100 to 700°C, more preferably 300 to 700°C and most preferably 450 to 650°C.

[00301] Aspect 29. The method, according to any one of aspects 22 to 28, in which the oxygen-containing gas supplied is air, oxygen-enriched air or oxygen gas.

[00302] Aspect 30. The method, according to any one of aspects 22 to 29, wherein the fuel comprises gaseous or liquid hydrocarbons, preferably natural gas, fuel oil or H2.

[00303] Aspect 31. The method, according to any one of aspects 22 to 30, in which the oxygen-containing gas is supplied in an amount that produces an excess of oxygen relative to Petition 870250076402, dated 08 / 28 / 2025, p. 85 / 136 78 / 106 quantity of oxygen for complete combustion of the fuel, and / or wherein the oxygen-containing gas is supplied in an amount wherein the value k is in a range of 0.01 to 10, preferably from 0.1 to 5, more preferably from 0.5 to 2 and even more preferably from 0.7 to less than 1.

[00304] Aspect 32. The method, according to any of the preceding aspects, in which the feedstock containing particulate carbon is injected through multiple inlets, preferably radial and perpendicular to the central longitudinal axis of the reactor.

[00305] Aspect 33. The method, according to any of the above aspects, in which the concentration of O2 in the hot gas stream is less than 5% by volume, preferably less than 4% by volume, more preferably 0.01 to 3% by volume and most preferably 0.1 to 2% by volume.

[00306] Aspect 34. The method, according to any of the aspects above, in which the carbon black obtained comprises recovered carbon black and new carbon black.

[00307] Aspect 35. The method, according to any of the preceding aspects, wherein the residence time is the time between the injection of the feedstock containing particulate carbon into the reactor and the cooling time of the product mixture, and is from 150 ms to 4 s, preferably from 200 ms to 3 s, more preferably from 250 ms to 2 s, and even more preferably from 250 ms to 1 s.

[00308] Aspect 36. The method, according to any of the preceding aspects, wherein the residence time of the feedstock containing particulate carbon is from 150 ms to 4 s, preferably from 200 ms to 3 s, more preferably from 250 ms to 2 s, and even more preferably from 250 ms to 1 s, wherein the residence time is calculated according to equation (1); V Petition 870250076402, dated 08 / 28 / 2025, page 86 / 136 79 / 106 Equation (1), where t is the residence time, V is the reaction volume (in m3) and Q is the volumetric flow rate (in m3*s'1).

[00309] Aspect 37. The method, according to aspect 36, wherein the volumetric flow rate is the volume of fluid after injection of the feedstock containing particulate carbon into the hot gas stream per second, preferably the fluid volume is calculated according to the ideal gas law according to equation (2) ÚRT $ ~ P Equation (2), where Q is the volumetric flow rate of the fluid (in m3*s'1), ri is the sum of the molar flow rates of the volatile gaseous substances N2, CO2, CO, H2O (in mol*s_1), R is the gas constant, i.e., 8.3145 JK“1-mol-1, T is the absolute temperature, P is the pressure.

[00310] Aspect 38. The method, according to any of aspects 35 to 37, the residence time is selected in such a way that the C,H-containing material in the particulate carbon-containing feedstock is completely pyrolyzed.

[00311] Aspect 39. The method, according to any of the preceding aspects, wherein the method further comprises (e) quenching the hot gas flow after injection according to step (d).

[00312] Aspect 40. The method, according to any of the preceding aspects, wherein the hot gas flow is quenched (and) when the transmittance at 425 nm of the carbon black obtained is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene. Petition 870250076402, dated 08 / 28 / 2025, p. 87 / 136 80 / 106

[00313] Aspect 41. The method, according to any of the preceding aspects, wherein the transmittance at 425 nm of the produced carbon black is measured and the cooling position is adjusted until the transmittance at 425 nm of the produced carbon black is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene.

[00314] Aspect 42. The method, according to any of the preceding aspects, in which the quenching position in the entrained flow reactor is selected such that the transmittance at 425 nm of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, in which the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene.

[00315] Aspect 43. The method, according to any of the preceding aspects, in which the feedstock containing particulate carbon is injected into the reactor at a mass flow rate of 2 to 50 kg / h per 130 L of the reactor reaction volume, preferably 5 to 40 kg / h per 130 L of the reactor reaction volume, more preferably 8 to 30 kg / h per 130 L of the reactor reaction volume, and even more preferably 10 to 20 kg / h per 130 L of the reactor reaction volume.

[00316] Aspect 44. The method, according to any of the preceding aspects, in which the reaction volume of the reactor is the reactor volume between the injection position of the feedstock containing particulate carbon and the cooling position.

[00317] Aspect 45. The method, according to any of the Petition 870250076402, dated 08 / 28 / 2025, page 88 / 136 81 / 106 aspects 2 to 44, in which deagglomeration is done by (i) acceleration of the raw material containing particulate carbon and / or (ii) application of shear forces, preferably using an extruder.

[00318] Aspect 46. The method, according to any one of aspects 2 to 45, in which deagglomeration is carried out in (i) a feeding and mixing device, preferably comprising a nozzle, and / or (ii) an extruder.

[00319] Aspect 47. The method, according to any one of aspects 2 to 46, in which deagglomeration is carried out in (i) a feeding and mixing device comprising a Laval nozzle.

[00320] Aspect 48. The method, according to any one of aspects 2 to 47, in which deagglomeration is carried out by subjecting the raw material containing particulate carbon to a jet of carrier gas.

[00321] Aspect 49. The method, according to any one of aspects 2 to 48, in which deagglomeration is carried out in a particle feeding and mixing device in a reactor comprising: (i) a carrier gas passage extending through said feeding and mixing device, (ii) at least one carrier gas inlet that is in fluid communication with said carrier gas passage, (iii) at least one particle inlet, (iv) a mixing chamber that is in fluid communication with said at least one particle inlet and with said carrier gas inlet, (v) a deagglomeration conduit that is in fluid communication with said mixing chamber, (vi) at least one outlet inlet for entrained particles from the carrier gas that were fed into the mixing chamber, in Petition 870250076402, dated 08 / 28 / 2025, p. 89 / 136 82 / 106 that at least one outlet is in fluid communication with the deagglomeration conduit, and (vii) means for accelerating and injecting a carrier gas flow into said mixing chamber.

[00322] Aspect 50. The method, according to any one of aspects 2 to 49, in which the feedstock containing deagglomerated particulate carbon is injected into the reactor at a pressure of 0.5 bar to 2 bar, preferably 0.7 bar to 1.5 bar, more preferably 0.8 to 1.3 bar and even more preferably 0.8 to 1.2 bar.

[00323] Aspect 51. The method, according to any of the preceding aspects, in which the feedstock containing particulate carbon is contained in a carrier gas.

[00324] Aspect 52. The method, according to any one of aspects 2 to 51, in which the feedstock containing deagglomerated particulate carbon is contained in a carrier gas.

[00325] Aspect 53. The method, according to any one of aspects 2 to 52, wherein the feedstock containing deagglomerated particulate carbon is comprised in a carrier gas and the carrier gas further comprises H2O and / or additives.

[00326] Aspect 54. The method, according to any one of aspects 2 to 53, wherein the feedstock containing deagglomerated particulate carbon is comprised in a carrier gas and the carrier gas further comprises H2O in an amount of 1 to 10% by volume, based on the total volume of the carrier gas comprising the feedstock containing deagglomerated particulate carbon.

[00327] Aspect 55. The method, according to any of the preceding aspects, in which said feedstock containing particulate carbon is injected into said entrained flow reactor by a plurality of inlets, preferably by a plurality Petition 870250076402, dated 08 / 28 / 2025, pp. 90 / 136 83 / 106 injection nozzles.

[00328] Aspect 56. The method, according to any of the preceding aspects, in which the feedstock containing particulate carbon is classified, preferably sieved, before the feedstock containing particulate carbon is injected into the reactor, preferably (a) the sieve has openings of 2000 μm, 1000 μm, 500 μm, 250 μm or 125 μm, preferably 500 μm, 250 μm or 125 μm, and / or (b) the sieve has openings of a size that retains particles larger than 2000 μm, larger than 1000 μm, larger than 500 μm, larger than 250 μm or larger than 125 μm, preferably larger than 500 μm, larger than 250 μm, or larger than 125 μm.

[00329] Aspect 57. The method, according to any of the preceding aspects, wherein at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the feedstock containing particulate carbon has a particle size less than 2 mm, preferably less than 1 mm, more preferably less than 500 µm and most preferably less than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00330] Aspect 58. The method, according to any of the preceding aspects, wherein at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the feedstock containing particulate carbon has a particle size smaller than 500 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00331] Aspect 59. The method, according to any of the preceding aspects, in which at least 70% by weight, preferably at least 80% by weight, more preferably at least Petition 870250076402, dated 08 / 28 / 2025, page 91 / 136 84 / 106 90% by weight, more preferably at least 98% by weight, of the feedstock containing particulate carbon has a particle size smaller than 1 mm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00332] Aspect 60. The method, according to any of the preceding aspects, wherein at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the particulate carbon-containing feedstock has a particle size less than 2 mm, preferably less than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00333] Aspect 61. Carbon black produced according to a method of any of the preceding aspects and / or (I) carbon black having a BET surface area of ​​80 to 90 m2 / g and a compressed oil absorption number of 58 to 69 mL / 100 g, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil; and / or (II) carbon black having a BET surface area of ​​70 to 85 m2 / g and a compressed oil absorption number of 59 to 70 mL / 100 g, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil; and / or (III) carbon black having a BET surface area of ​​80 to 96 m2 / g and an absorption number Petition 870250076402, dated 08 / 28 / 2025, p. 92 / 136 85 / 106 compressed oil concentration of 60 to 69 mL / 100 g, wherein the BET surface area is measured according to ASTM D6556-21, the compressed oil absorption number is measured according to ASTM D3493-20 using paraffinic oil; and / or (IV) carbon black having a BET surface area of ​​120 to 138 m2 / g and a compressed oil absorption number of 58 to 69 mL / 100 g, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil; and / or (V) carbon black having a BET surface area of ​​82 to 95 m2 / g and a compressed oil absorption number of 59 to 70 mL / 100 g, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil.

[00334] Aspect 61b. Carbon black according to aspect 61, wherein (I) Carbon black (I) preferably has a BET surface area of ​​85 to 88 m2 / g, and preferably a compressed oil absorption number of 61 to 64 mL / 100 g, preferably an STSA surface area of ​​72 to 82 m2 / g, more preferably an STSA surface area of ​​76 to 79 m2 / g, preferably volatiles of 2.1 to 2.7% by weight, more preferably volatiles of 2.3 to 2.5% by weight, preferably a transmittance at 425 nm in toluene greater than 50%, more preferably a transmittance at 425 nm in toluene greater than 77%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number Petition 870250076402, dated 08 / 28 / 2025, pp. 93 / 136 86 / 106 moisture content is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D655621, wherein volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene; and / or (II) carbon black (II) preferably has a BET surface area of ​​77 to 79 m2 / g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​68 to 78 m2 / g, more preferably an STSA surface area of ​​71 to 73 m2 / g, preferably a compressed oil absorption number of 58 to 69 mL / 100 g, more preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably volatiles of 2.0 to 2.6% by weight, more preferably volatiles of 2.2 to 2.4% by weight, preferably a transmittance at 425 nm in toluene greater than 40%,more preferably a transmittance at 425 nm in toluene greater than 56%, wherein the BET surface area is measured in accordance with ASTM D655621, the tablet oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D6556-21, wherein the volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 against toluene; and / or (III) carbon black (III) preferably has a BET surface area of ​​89 to 92 m2 / g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​79 to 87 m2 / g, more preferably an STSA surface area of ​​82 to 84 m2 / g, preferably volatiles of 2.2 to 2.9% by weight, more preferably volatiles of 2.5 to 2.7% by weight, preferably a transmittance at 425 nm in toluene superior, Petition 870250076402, dated 08 / 28 / 2025, pp. 94 / 136 87 / 106 or 40%, more preferably a transmittance at 425 nm in toluene greater than 62%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D655621, wherein the volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene;and / or (IV) Carbon black (IV) preferably has a BET surface area of ​​127 to 130 m² / g, preferably a compressed oil absorption number of 62 to 64 mL / 100 g, preferably an STSA surface area of ​​82 to 95 m² / g, more preferably an STSA surface area of ​​87 to 89 m² / g, preferably volatiles of 2.6 to 3.2% by weight, more preferably volatiles of 2.8 to 3.0% by weight, preferably a transmittance at 425 nm in toluene greater than 60%, more preferably a transmittance at 425 nm in toluene greater than 80%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the surface area STSA is measured in accordance with ASTM D655621, where volatiles are measured at 950°C for 7 min, as described in the descriptive report, and transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene;and / or (V) Carbon black (V) preferably has a BET surface area of ​​86 to 89 m2 / g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​70 to 82 m2 / g, more preferably an STSA surface area of ​​76 to 78 m2 / g, preferably volatiles of 1.8 to 2.4% by weight, more preferably volatiles of 2.0 to 2.2% by weight, preferably a transmittance at 425 nm in toluene above; Petition 870250076402, dated 08 / 28 / 2025, pp. 95 / 136 88 / 106 or 60%, more preferably a transmittance at 425 nm in toluene greater than 80%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is measured in accordance with ASTM D655621, wherein the volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene.

[00335] Aspect 62. A composition comprising (A) an elastomeric polymeric material and (B) carbon black obtained in accordance with any one of aspects 1 to 61 and 61b.

[00336] Aspect 63. An article made in or comprising composition in accordance with aspect 62.

[00337] Aspect 64. Use of a feedstock containing particulate carbon for the manufacture of carbon black in an entrained flow reactor.

[00338] Aspect 65. Use in accordance with aspect 64, wherein at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the particulate carbon-containing feedstock has a particle size less than 2 mm, preferably less than 1 mm, more preferably less than 500 µm and most preferably less than 250 µm, wherein the particle size is measured in accordance with ASTM D 1511-12 2017).

[00339] Aspect 66. Use in accordance with either of aspects 64 and 65, wherein the residence time of the feedstock containing particulate carbon is from 150 ms to 4 s, preferably from 200 ms to 3 s, more preferably from 250 ms to 2 s, and even more preferably from 250 ms to 1 s, wherein the residence time is calculated Petition 870250076402, dated 08 / 28 / 2025, pp. 96 / 136 89 / 106 according to equation (1); v tr= —rQ Equation (1), where Léo residence time, V is the volume of the reaction volume (in m3) and Q is the volumetric flow rate (in m3*s'1).

[00340] Aspect 67. Use in accordance with any of aspects 64 to 66, wherein raw material containing deagglomerated particulate carbon is used.

[00341] Aspect 68. A method for adjusting the cooling position in an entrained flow reactor for the production of carbon black from a feedstock containing particulate carbon, comprising: I) Injecting a feedstock containing particulate carbon into a hot gas stream of an entrained flow reactor, where the hot gas stream has a temperature of at least 800°C, II) tempering of the hot gas stream that makes up the carbon black produced, II) to measure the transmittance of the carbon black produced, III) Adjust the cooling position in the entrained flow reactor until the transmittance of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 relative to toluene. EXAMPLES Example 1: Rubber granules

[00342] The experiments in Example 1 are carried out in a small-scale furnace reactor, as shown in Figure 1. The furnace reactor comprises a combustion chamber, a point of... Petition 870250076402, dated 08 / 28 / 2025, page 97 / 136 90 / 106 constriction and a tunnel. The constriction point reduces the diameter to 45 mm. Downstream of the constriction point, a reactor tunnel with a diameter of 200 mm and a length of 4200 mm is constructed.

[00343] The rubber granules were injected into the furnace reactor at the throttling point by means of a feeding and mixing device with a nozzle, as shown in Figure 2. The reaction volume of the reactor was approximately 130 liters. The reaction volume was the reactor volume between the raw material injection position and the quenching position. The feeding and mixing device deagglomerated the rubber granules by accelerating the raw material containing carbon particles. However, the present invention is not limited to the feeding and mixing device shown in Figure 1, so other feeding and mixing devices may be used. The rubber granules, i.e., Gummigranulat 0.0 - 0.5 mm (Article No. 005GUM), used in the experiments, were obtained from ESTATO Umweltservice GmbH (ESTATO), Germany. The rubber granules were derived from used tires and comprise synthetic rubber (SBR) and natural rubber (NR).The particle fractions are shown in Table 1. Furthermore, the weight-average particle diameter (Dw50) was approximately 400 µm, measured according to ASTM D 1511-12 2017. However, it is also possible to use different feedstocks containing particulate carbon, such as plastic granules or biomass-based granules. Table 1: Distribution of ESTATO rubber granulate particles, measured according to ASTM D 1511-12 2017). Particle fraction < 0.125 mm 2.0% by weight Particle fraction 0.125 - 0.25 mm 9.6% by weight Particle fraction 0.25 - 0.50 mm 34.5% by weight Particle fraction 0.50 - 1.0 mm 45.1% by weight Petition 870250076402, dated 08 / 28 / 2025, pp. 98 / 136 91 / 106 Fraction of particles 1.0 - 2.0 mm 8.8% by weight Fraction of particles < 2.0 mm 0.0% by weight

[00344] The characterization of ESTATO rubber granules is shown in Table 2. Table 2: Characterization of ESTATO rubber granules. Property Measurement Unit Value Carbon mass fraction See method below % 87.623 Hydrogen mass fraction See method below % 7.767 Nitrogen mass fraction See method below % 0.396 Sulfur mass fraction See method below % 2.022 Oxygen mass fraction See method below % 2.191 Water content ASTM D 4928-122018) % 2.19 Ash content ASTM D 1506-99 at 550°C, 16 h % 11.29 Gross Calorific Value ASTM D 4809:2018 MJ / kg 35.121

[00345] In addition, rubber granules contain various metals in a mass fraction of about 300 ppm. For example, zinc and iron. Determination of CHNS content using elemental analyzer

[00346] The mass fraction of carbon, the mass fraction of hydrogen, the mass fraction of nitrogen, and the mass fraction of sulfur are measured using an elemental analyzer with thermal conductivity and an infrared detector. The analyzer is a device for the fully automatic quantitative analysis of the above elements. The combustion tube is heated to a temperature of 1100°C and the reduction tube to 850°C. First, a blank measurement is performed. A Petition 870250076402, dated 08 / 28 / 2025, page 99 / 136 92 / 106 The carbon peak area must have a value < 50, the hydrogen peak area a value < 300, the nitrogen peak area a value < 50, and the sulfur peak area a value < 350. Otherwise, the individual adsorption columns are heated, and then the blank measurements are restarted. The blank measurement is calculated as follows: b = Σ> n, where b is the blank measurement, bi is the peak area of ​​the respective blank measurement, n is the number of blank measurements, and i is an index from 1 to n.

[00347] Blank measurement compensation is calculated as follows, acomp. = a - b, where acomp. is the compensated peak area, a is the measured peak area and b is the blank measurement value.

[00348] Next, the daily factor is measured. For this, 3 mg of sulfanilamide and 3 mg of low-level standard (e.g., carbon black standard) are weighed into each of the 8 tin capsules. After weighing, the respective sample is placed in the capsule press, covered with helium for 35 seconds, and then cold-sealed. Subtracting the blank value, the known theoretical concentration of the element in the standard samples is placed relative to the actually calculated concentration of the element. This results in the daily factor, which should be between 0.9 and 1.1. Otherwise, these measurements should be repeated with newly opened standards. Otherwise, a new calibration should be performed according to the manufacturer's instructions.

[00349] The daily factor is calculated as follows, f _ ctheor. cact. Petition 870250076402, dated 08 / 28 / 2025, pp. 100 / 136 93 / 106 Where f is the daily factor, ctheor. is the theoretical factor, and Cact. is the actual calculated elemental concentration.

[00350] Next, 8 tin capsules, each containing 5 mg ± 1 mg of the desired measured component, such as rubber granules, are weighed. After weighing the respective samples, they are placed in the capsule press, covered with helium for 35 sec, and then cold-soldered.

[00351] For the measurement, the combustion tube is enriched with O2. The elements C, H, Ne, and S burn to form CO2, H2O, NOx, SO2, and SO3. The bound halogen in the sample reacts to form volatile halogen compounds. In addition, there are WO3 granules in the combustion tube that provide more O2 as a catalyst, prevent the formation of non-volatile sulfates, and bind interfering alkaline and alkaline-earth elements. The carrier gas stream is fed into the reduction tube with Cu packing. Nitrogen oxides (NOx) are completely reduced to N2 in contact with the copper. SO3 is reduced to SO2. Volatile halogen compounds are bound to the silver wool.

[00352] N2 is not adsorbed and enters the thermal conductivity detector as the first measurement component; CO2, H2O, and SO2 are adsorbed in their respective adsorption columns.

[00353] Next, the adsorption columns are brought, one after the other, to the desorption temperature, so that CO2 and then H2O, as a carrier gas, enter the thermal conductivity detector and SO2 enters the infrared detector. Depending on the type and concentration of the components, the detector emits an electrical signal that is digitized and integrated. The measurement signal is recorded as a function of time and displayed as an integral value. The absolute content of elements in the sample is calculated from this integral value of the individual measurement peaks and calibration factors. Petition 870250076402, dated 08 / 28 / 2025, pp. 101 / 136 94 / 106

[00354] The concentration of the element is calculated according to the following equation a*100*fc =-------w , where c is the elemental concentration (in %), a is the absolute content of the element (in mg), f is the daily factor and w is the actual quantity of the sample. Determination of O content using an elemental analyzer.

[00355] Depending on the oxygen concentration, an electrical signal is transmitted from the thermal conductivity detector (WLD) of the elemental analyzer to a microcontroller and then displayed as an integral value. From the integral value of the measurement peaks and the calibration factor, the absolute elemental content of the sample is concluded.

[00356] The pyrolysis tube is heated to a temperature of 1050°C. First, a blank measurement is performed. The oxygen peak area should have a maximum value of 200. If the blank value is not less than 200, the CO adsorption column should be heated (260°C, CO desorption 150°C). After successful measurement of the blank values, the average value of the blank value areas is calculated.

[00357] The blank measurement is calculated as follows: b = ^bi n, where b is the blank measurement, bi is the peak area of ​​the respective blank measurement, n is the number of blank measurements, and i is an index from 1 to n.

[00358] Next, the daily factor is measured. For this, 3 mg of acetanilide are weighed into each of the 8 tin capsules. After weighing the respective sample, it is placed in the capsule press, covered with helium for 35 seconds, and then cold-sealed. Subtracting Petition 870250076402, dated 08 / 28 / 2025, pp. 102 / 136 95 / 106 the value of the blank, the known theoretical concentration of the element from the standard samples is placed relative to the actually calculated concentration of the element. This results in the daily factor, which should be between 0.9 and 1.1. Otherwise, these measurements should be repeated with newly opened standards. Otherwise, a new calibration should be performed according to the manufacturer's instructions.

[00359] The daily factor is calculated as follows, f _ ctheor. Oact, where f is the daily factor, ctheor. is the theoretical factor, and cact. is the actual calculated elemental concentration.

[00360] Next, 8 tin capsules, each containing 5 mg ± 1 mg of the desired measured component, such as rubber granules, are weighed. After weighing the respective samples, they are placed in the capsule press, covered with helium for 35 s, then cold-soldered. The samples are then measured.

[00361] The concentration of the element is calculated according to the following equation a*100*fc =-------w , where c is the elemental concentration (in %), a is the absolute content of the element (in mg), f is the daily factor and w is the actual quantity of the sample. Reaction conditions in the furnace reactor

[00362] The reaction conditions for the manufacture of carbon black are shown in Table 3. The temperature of the hot gas stream after the injection of the raw material is calculated as described in the descriptive report. As mentioned earlier, the temperature (absolute temperature) can also be measured with a pyrometer. In addition, residence times are calculated for particles with di Petition 870250076402, dated 08 / 28 / 2025, pp. 103 / 136 96 / 106 diameters of 0.5 mm and 1 mm. A pyrolysis modeling program was used for the calculation. Table 3: Reaction conditions in the furnace reactor. Experiment A1 A2 A3 A4 A5 Combustion air flow (STP) l / m3 / h 150 150 150 150 150 Natural gas flow (STP) / m3 / h 10.3 10.8 12.1 10.9 13.8 K2 value 0.66 0.69 0.78 0.70 0.89 Combustion air temperature upstream of the combustion chamber / °C 354 450 400 447 341 Natural gas temperature upstream of the combustion chamber / °C 21 21 21 21 21 Nitrogen purge flow (STP) / m3 / h 14 10.5 8.7 8 8.3 Rubber granulate mass flow / kg / h 25 16 18 25 11 Molar fraction of O2 Dosing point of the dosing reactor / % n / D 5.5 5.7 4.2 6.7 Calculated temperature of the hot gas flow / °C 1493 1633 1626 1580 1677 Residence time / s 0.394 0.375 0.382 0.39 0.376 ideal for particles with a diameter of 0.5 mm at the calc. temperature / s 0.35 0.32 0.32 0.32 0.31 Ideal residence time for particles with a diameter of 1 mm at the calc. temperature / s 1.32 1.125 1.125 1.22 1.1 1273.15 K and 101325 Pa2. The value k is defined by the ratio between the stoichiometric quantity of The amount of O2 required for the complete stoichiometric combustion of the fuel and the amount of O2 supplied. Table 2: continued Petition 870250076402, dated 08 / 28 / 2025, pp. 104 / 136 97 / 106 Experiment A6 A7 A8 A9 A10 Combustion air flow (STP) / m3 / h 150 150 150 150 150 Natural gas flow (STP) / m3 / h 13.9 12.4 10.8 12.4 12.4 K value 0.89 0.80 0.69 0.80 0.80 Combustion air temperature upstream of the combustion chamber / °C 456 398 350 405 390 Natural gas temperature upstream of the combustion chamber / °C 21 21 21 21 21 Nitrogen purge flow (STP) / m3 / h 5.7 7.1 6.5 6.7 7.5 Rubber granulate mass flow / kg / h 11 18 16 18 18 Molar fraction of O2 at the dosing point of the dosing reactor / % 7.3 5 4.9 5 3.9 Calculated temperature of the hot gas flow / °C 1763 1640 1592 1645 1632 Residence time / s 0.367 0.383 0.391 0.383 0.383 Ideal residence time for particles with a diameter of 0.5 mm at the calc. temperature / s 0.28 0.315 0.32 0.31 0.32 Ideal residence time for particles with a diameter of 1 mm at the calc. temperature / s 1.05 1.11 1.22 1.125 1.125

[00363] After injection of the granulated rubber raw material, the reaction was stopped with water and the resulting carbon black was dried and ground to obtain an average particle size of about 5 µm. The carbon black obtained according to the invention (see Experiments A1 to E12) was compared to a standard N660 carbon black and to recovered carbon black (rCB). The rCB was recovered from pyrolysis of rubber granules.

[00364] The temperature in the combustion chamber, that is, the temp Petition 870250076402, dated 08 / 28 / 2025, pp. 105 / 136 98 / 106 The temperature of the hot combustion gases was controlled by the temperature of the combustion air upstream of the combustion chamber (i.e., the temperature of the oxygen-containing gas). The k value was controlled by the flow of natural gas (fuel) in the combustion chamber.

[00365] The carbon black produced comprises approximately 53% by weight of recovered carbon black, approximately 27% by weight of new carbon black, and approximately 20% by weight of ash. The recovered carbon black comprises coke. Because rubber granules are used in an entrained flow reactor process, it is possible not only to recover carbon black but also to produce new carbon black derived from rubber. Thus, the ash content is lower compared to carbon black recovered from REOIL (RCB615, approximately 23.2% by weight of ash). The ash content can be measured according to ASTM D 1506-99 at 550°C, 16 h.

[00366] The carbon black obtained in each experiment was characterized and the results are shown in Table 4. Table 4: Characterization of the carbon black obtained Experiment B1 B2 B3 B4 B5 B6 B7 Carbon black N550 3 N660 4 rCb 5 A1 A2 A3 A4 Aggregate size6, numerical mean / nm 212 208 98 n / D n / D 46 46 Aggregate size6, weight mean / nm 167 n / D n / D 102 106 Aggregate size6, weight mode / nm 172 156 n / D n / D 70 74 Specific surface area7 (VSA) / m2 / g 24 n / D n / D 42.6 41.3 Volatiles8 / % by weight 4.5 n / D n / D 2.4 2.3 Surface area BET9 / m2 / g 39 35.1 72.4 n / D 117.4 86.6 78.2 Surface area STSA10 / m2 / g 38.75 34.55 60.9 n / A 91 77.8 72.1 Petition 870250076402, dated 08 / 28 / 2025, pp. 106 / 136 99 / 106 Iodine adsorption11 42.7 36.6 94.5 n / D n / D 101.1 77.8 pH value12 8.7 8.4 7.32 n / D n / D 7.42 7.38 Compressed oil absorption number (CO-AN)13 / ml / 100g 83.9 72 80.2 n / D n / D 62.2 64.4 Oil absorption number (OAN)14 120.95 90.35 92.3 n / D n / D 64 68.6 Transmittance15 / % 97 92.7 n / D n / D 94.9 78.7 57.5 3N550 carbon black obtained from liquid feedstocks, Orion Engineered Carbons GmbH; 4N660 carbon black obtained from liquid feedstocks, Orion Engineered Carbons GmbH; 5rCB 2 recovered carbon black, REOIL SP Z OO6A. The aggregate size distribution was measured as described below. 7. The specific surface area (SFA) was measured as described below. 8 volatile compounds were measured at 950°C for 7 min, as described below.9 BET was measured in accordance with ASTM D6556-21. The surface area of ​​the STSA was measured in accordance with ASTM D655621. 11The iodine adsorption number was measured in accordance with ASTM D1510-21. 12 is measured according to ASTM D1512-21, Test Method B - Sonic Paste13The compressed oil absorption number (COAN) was measured according to ASTM D3493-20 (using paraffinic oil)14The oil absorption number (OAN) was measured according to ASTM D2414-19 (using paraffinic oil)15The transmittance at 425 nm in toluene (Toluene Extract Transmittance) was measured according to ASTM D 1618-18 against toluene. Table 4: continued Petition 870250076402, dated 08 / 28 / 2025, pp. 107 / 136 100 / 106 Experiment B8 B9 B10 B11 B12 B13 Carbon black A5 A6 A7 A8 A9 A10 Aggregate size6, numerical mean / nm 42 41 47 49 n / D n / D Aggregate size6, weight mean / nm 105 102 108 105 n / D n / D Aggregate size6, weight mode / nm 74 73 76 72 n / D n / D Specific surface area7 (VSA) / m2 / g 42 43.9 40.2 40.6 n / D n / D Volatiles8 / % by weight 2.6 2.9 2.2 2.1 n / D n / D Surface area BET9 / m2 / g 90.9 128.6 n / D 87.5 84.2 79.5 Surface area STSA10 / m2 / g 83.2 88.4 n / D 77.1 77 75.1 Iodine adsorption11 94.4 129.2 93.2 99.7 n / D n / D pH value12 7.36 7.06 7.23 8.01 n / D n / D Compressed oil absorption number (COAN)13 / ml / 100g 64.5 63.4 63.7 64.3 n / D n / D Oil absorption number (OAN)14 68 66.5 70.6 67.2 n / D n / D Transmittance 15 / % 63 95 52.8 86 66.9 48.6 The aggregate distribution of size

[00367] All test results are analyzed according to ISO 15825:2016, using a Brookhaven BI-DCP disc centrifuge with red light diode. The cited test results are provided in the Brookhaven software after the necessary parameter adjustments described in the Computer and Software Configuration section of ISO 185825:2017-03. Specific surface area (VSA)

[00368] The specific surface area of ​​a tested sample is available in the Brookhaven software. After testing the sample and reviewing the results, click on Detailed Results and read the area value. Petition 870250076402, dated 08 / 28 / 2025, pp. 108 / 136 101 / 106 specific surface area in g2 on a computer screen. Volatiles at 950°C

[00369] Volatiles at 950°C were measured using a thermogravimetric instrument from the Faculty of Technology. LECO Instrumente GmbH (TGA-701) according to the following protocol: The pans were dried at 650°C for 30 min. The carbon black materials were stored in a desiccator equipped with a desiccant before measurements. The baked pans were loaded into the instrument, tared, and filled with between 0.5 g and 10 g of carbon black material. Then, the TGA instrument oven loaded with the sample-filled pans was gradually heated to 105°C by automated software control, and the samples were dried until a constant mass was reached. Subsequently, the pans were closed with lids, the oven was purged with nitrogen (99.9 vol%) and heated to 950°C. The oven temperature was maintained at 950°C for 7 min. The volatile content at 950°C was calculated using the following equation: ,, „ nifantej da aauecimenta)—m(grandparents 7 minutes aGBO'T) Volatile =—--------------——------------· 100%. nifanísj da aqitffciniffnto'} Results

[00370] It was surprisingly found that it is possible to use feedstock containing particulate carbon in an entrained flow reactor process. As can be seen in Table 3, the carbon obtained exhibits desirable properties compared to standard carbon black products obtained from feedstock containing liquid carbon.

[00371] Furthermore, the aggregate size, as well as the aggregate surface area, are smaller compared to the aggregate size and aggregate surface area of ​​the recovered carbon blacks. This indicates that the resulting carbon black has a lower coke content. The specific surface area of ​​the size measurement Petition 870250076402, dated 08 / 28 / 2025, pp. 109 / 136 A 102 / 106 aggregate size also indicates the amount of coke present in the carbon black. Furthermore, a large aggregate size is also an indication of a high coke content.

[00372] Furthermore, as can be observed in Table 3, the residence time of A6 is 0.367 s if the temperature of the hot gas stream was 1763°C. It is believed that the higher temperature results in an optimum residence time of 0.28 s for particles with a diameter of 0.5 mm and 1.05 s for particles with a diameter of 1 mm. The transmittance in experiment B9 using A6 is 95%. Transmittance is an indicator of complete pyrolysis of the feed material or of C,H-containing compounds in the feed. Therefore, it is believed that a higher temperature and a longer residence time are beneficial for the manufacture of carbon black from particles. Example 2: Rubber compounds

[00373] The preparation of rubber compounds and rubber testing are described below. A general process for the production of rubber compounds and their vulcanizates is described in the book Rubber Technology Handbook, W. Hofmann, Hanser Verlag, 1994.

[00374] The rubber compositions are mentioned in Table 5. ESBR Buna SB 1500 was introduced into a GK1.5E laboratory mixer with a Harburg Freudenberger interlocking PES5 rotor geometry and milled for 30 seconds at a chamber temperature of 40°C, a filling factor of 0.66, and a rotor speed of 45 rpm. Subsequently, half the volume of carbon black, ZnO, and stearic acid were added under milling. After 90 seconds, the other half volume of carbon black and 6PPD were added. After another 90 seconds, the ram was lifted and cleaned, and the batch was mixed for another 90 seconds. The total mixing time in the internal mixer was 5 minutes, after which the batch was discarded. Petition 870250076402, dated 08 / 28 / 2025, pp. 110 / 136 103 / 106 of the batch was placed in an open mill for cooling and further distributive mixing. The batch temperature did not exceed 160°C during the first mixing stage. The batch was left to stand overnight.

[00375] During the second and final mixing stage, sulfur and accelerator (Vulkacit CZ / EG-Z) were then added in the indicated quantities to the masterbatch obtained in the first mixing stage. The resulting mixture was milled in the GK1.5E mixer with a chamber temperature of 40°C and a filling factor of 0.64 for 2 minutes. The rotor speed was 30 rpm and it was ensured that the batch temperature did not exceed 110°C. Finally, the mixture was discharged from the inner mixer and processed again in an open mill. The resulting vulcanizable compositions (green compounds) were cured for between 11 and 15 minutes (C1: 15 min, C2: 12 min, C3: 12 min, C4: 12 min, C5: 11 min, C6: 12 min, C7: 12 min, C8: 11 min, C9: 11 min) at a temperature of 165°C. Table 5: Rubber compositions using different carbon blacks, as observed in Table 6. Unit Composition Rubber 16 phr 100 Carbon black 17 phr 50 ZnO 21 phr 3 Stearic acid 22 phr 2 6PPD 18 phr 1 Sulfur 19 phr 1.5 CBS 20 phr 1.5 16ESBR rubber, Buna SB 1500, Resinex Deutschland GmbH17Carbon black: N660, N550, rCB or from Experiments A3 to 5 and A8 to A10 (see table 6)186PPD, VULKANOX 4020 / LG, Brenntag GmbH19Sulphur, MAHLSCHWEFEL 80 / 90° unbeolt, Avokal GmbH20CBS, VULKACIT CZ / EG-C, Lanxess NV Petition 870250076402, dated 08 / 28 / 2025, pp. 111 / 136 104 / 10621ZnO, ZNO RS RAL 844 C, Norkem BV22Stearic Acid, Palmera B 1804, Caldic Deutschland GmbH

[00376] The properties of the specimens were measured and the results are indicated in Table 6. The results are compared with carbon blacks produced using a liquid carbon black feedstock (N660 and N550) and recovered rCB carbon blacks. Table 6: Properties of carbon black produced in rubber compounds. Experiment C1 C2 C3 C4 Carbon black N6603 N5504 rCb5 A3 Loss factor tan(d)23 0.125 0.139 0.142 0.156 Relative peak area of ​​topography24 / % 0.63 0.2 1.01 6.91 Tensile strength 25 / Mpa 20.5 24.1 23.3 26.3 Elongation at break26 / % 474 503 631 665 Abrasion27 / mm3 96 82 111 107 Modulus 300% 28 / Mpa 11.7 13 6.7 5.5 Ball rebound29 68.2 65.1 66 62.2 Tear resistance GRAVES30 18.2 21.5 17.9 18.6 23The loss factor tan(d) was measured as described below. 24. The area of ​​the peak relative to the topography was measured as described below. 25A tensile strength was measured according to ISO 37 - 2012, S2. 26. Elongation at break was measured ISO 37 - 2012, S2. 27A abrasion was measured at 23°C DIN ISO 4649:2014-03, 10 N. 28300% was measured according to ISO 37 - 2012, S2. 29The ball rebound was measured at 60°C ASTM D 2632:2015. 30A GRAVES tear resistance was measured according to DIN ISO 341:2016-09, method B, variant (b). Petition 870250076402, dated 08 / 28 / 2025, pp. 112 / 136 105 / 106 Experiment C5 C6 C7 C8 C9 Carbon black A4 A5 A6 A7 A8 Loss factor tan(d) 0.153 0.155 0.159 0.154 0.152 Relative peak area of ​​topography / % 4.43 3.59 6.13 2.7 3.2 Tensile strength / MPa 25.4 25 25.2 25.6 26.6 Elongation at break / % 629 655 651 612 665 Abrasion / mm³ 105 114 112 107 117 Modulus 300% / MPa 6.1 5.8 5.9 6.9 5.6 Ball rebound 62.2 62.4 61.6 61.7 62.8 Resistance to tear BASS 30 19.1 19.7 19.1 20.2 18.4 Topography of the peak area relative

[00377] The relative area of ​​the topography peak is a measure of filler dispersion determined by means of surface topography, including the Medalia correction, according to the procedure described in A. Wehmeier, Filler Dispersion Analysis by Topography Measurements, Technical Report TR 820, Degussa GmbH, as well as in A. Wehmeier, Entwicklung eines Verfahrens zur Charakterisierung der Füllstoffdispersion in Gummimishungen mittels einer Oberflachentopographie, Thesis, 1998 at the University of Applied Sciences of Münster, and DE 199 17975 C2. Loss factor tan(d)

[00378] The above-mentioned values ​​and the loss factor tan(d) were measured according to DIN 53 513 in strain-controlled mode (1 ± 0.5 mm) or force-controlled mode (50 N ± 25 N) on a cylindrical sample 10 mm high and 10 mm in diameter) at 60°C with a frequency of 16 Hz. Results Petition 870250076402, dated 08 / 28 / 2025, pp. 113 / 136 106 / 106

[00379] The example reveals that the carbon blacks produced according to the invention (carbon blacks A3-A5, A8-A10) can be advantageously used in a rubber compound (Experiment C5 to C10). The produced carbon blacks have a low tan(d) loss factor, combined with high topography and high tensile strength. Furthermore, the elongation at break is advantageously between 612 and 665%. The ball rebound of the produced carbon blacks is comparable to the ball rebound of N660 and N550 carbon blacks.

[00380] It will be appreciated that various modifications can be made, and that many changes can be made to the preferred embodiments without departing from the principle of the invention. Petition 870250076402, dated 08 / 28 / 2025, pp. 114 / 136

Claims

1 / 9 CLAIMS 1. A method for producing carbon black from a feedstock containing particulate carbon in an entrained flow reactor having a flow passage along a central longitudinal axis of the reactor, characterized in that it comprises: (a) providing a hot gas stream, (b) providing a feedstock containing particulate carbon, and (d) injecting the feedstock containing carbon particles into the hot gas stream to form carbon black, wherein the hot gas stream has a temperature of at least 800°C.

2. Method according to claim 2, characterized in that the raw material containing particulate carbon comprises rubber granules, plastic granules and / or biomass-based granules, preferably the raw material containing particulate carbon comprises rubber granules, wherein the rubber granules comprise carbon black.

3. A method according to claim 1 or 2, characterized in that at least 70% by weight, preferably at least 80% by weight, more preferably at least 90% by weight, most preferably at least 98% by weight, of the particulate carbon-containing raw material has a particle size smaller than 2 mm, preferably smaller than 1 mm, more preferably smaller than 500 µm and most preferably smaller than 250 µm, the particle size being measured in accordance with ASTM D 1511-12 2017.

4. Method, according to any one of claims 1 to 3, characterized in that the particle size distribution of the raw material containing particulate carbon is measured as per Petition 870250076402, dated 08 / 28 / 2025, page 1. 115 / 136 2 / 9 in accordance with ASTM D 1511-12 2017) and (a) Sieve No. 10 retains 1 to 10% by weight, preferably 1 to 8% by weight, more preferably 1 to 5% by weight, and even more preferably 1 to 3% by weight of the raw material containing carbon particles, and / or (b) Sieve No. 18 retains 1 to 25% by weight, preferably 2 to 20% by weight, more preferably 4 to 15% by weight, and even more preferably 5 to 12% by weight of the raw material containing carbon particles, and / or (c) Sieve No. 35 retains 10 to 80% by weight, preferably 15 to 70% by weight, more preferably 20 to 60% by weight, and even more preferably, 25 to 55% by weight of the raw material containing carbon particles,and / or (d) The No. 60 sieve retains 5 to 70% by weight, preferably 10 to 60% by weight, more preferably 15 to 50% by weight, and even more preferably 20 to 45% by weight of the raw material containing carbon particles, and / or (e) The No. 120 sieve retains 1 to 80% by weight, preferably 7 to 70% by weight, more preferably 5 to 60% by weight, and even more preferably 7 to 50% by weight of the raw material containing carbon particles, and / or (f) The lower receiving tray comprises less than 4% by weight, preferably less than 3% by weight, more preferably 0 to 2% by weight, and even more preferably 0.01 to 1% by weight of the raw material containing particulate carbon.

5. Method, according to any one of claims 1 to 4, characterized in that the hot gas flow is obtained by electrical preheating, plasma heating and combustion of a fuel gas containing oxygen, and / or the entrained flow reactor is a furnace reactor. Petition 870250076402, dated 08 / 28 / 2025, pp. 116 / 136 3 / 9 6. A method according to any one of claims 1 to 5, characterized in that the feedstock containing particulate carbon is sorted, preferably sieved, before the feedstock containing particulate carbon is injected into the reactor, preferably (a) the sieve has openings of 2000 µm, 1000 µm, 500 µm, 250 µm or 125 µm, preferably 500 µm, 250 µm or 125 µm, and / or (b) the sieve has openings with a size that retains particles with a size greater than 2000 µm, greater than 1000 µm, greater than 500 µm, greater than 250 µm or greater than 125 µm, preferably greater than 500 µm, greater than 250 µm, or greater than 125 µm.

7. Method, according to any one of claims 1 to 6, characterized in that the residence time of the feedstock containing particulate carbon is from 150 ms to 4 s, preferably from 200 ms to 3 s, more preferably from 250 ms to 2 s, and even more preferably from 250 ms to 1 s, wherein the residence time is calculated according to equation (1); V Equation (1), wherein t is the residence time, V is the volume of the reaction volume (in m3) and Q is the volumetric flow rate (in m3*s'1).

8. A method according to any one of claims 1 to 7, characterized in that the quenching position in the entrained flow reactor is selected such that the transmittance at 425 nm of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene.

9. Method, according to any of the claims Petition 870250076402, dated 08 / 28 / 2025, pp. 117 / 136 4 / 9 1 to 8, characterized in that the feedstock containing particulate carbon is injected into the reactor with a mass flow rate of 2 to 50 kg / h per 130 L of the reactor's reaction volume, preferably 5 to 40 kg / h per 130 L of the reactor's reaction volume, more preferably 8 to 30 kg / h per 130 L of the reactor's reaction volume and, even more preferably, 10 to 20 kg / h per 130 L of the reactor's reaction volume.

10. Method, according to any one of claims 1 to 9, characterized in that Step (b) further comprises the deagglomeration of the feedstock containing particulate carbon and, in Step (d), the deagglomerated feedstock containing particulate carbon is injected into the hot gas stream to form carbon black, wherein the deagglomeration is done (i) by accelerating the feedstock containing particulate carbon and / or (ii) by applying shear forces, preferably using an extruder.

11. Carbon black, characterized in that it is produced according to the method as defined in any one of claims 1 to 10, and / or (I) carbon black having: a BET surface area of ​​80 to 90 m² / g, preferably a BET surface area of ​​85 to 88 m² / g, and a compressed oil absorption number of 58 to 69 mL / 100 g, preferably a compressed oil absorption number of 61 to 64 mL / 100 g, preferably an STSA surface area of ​​72 to 82 m² / g, more preferably an STSA surface area of ​​76 to 79 m² / g, preferably volatiles of 2.1 to 2.7% by weight, more preferably volatiles of 2.3 to 2.5% by weight, preferably a transmittance at 425 nm in toluene. 870250076402, dated 08 / 28 / 2025, p. 118 / 136 5 / 9 greater than 50%, more preferably a transmittance of 425 nm in toluene greater than 77%, and the BET surface area is measured in accordance with ASTM D6556-21,The compressed oil absorption number is measured according to ASTM D3493-20 using paraffinic oil, the STSA surface area is measured according to ASTM D6556-21, with volatiles measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 with respect to toluene; and / or (II) carbon black having: a BET surface area of ​​70 to 85 m2 / g, preferably a BET surface area of ​​77 to 79 m2 / g, and a compressed oil absorption number of 59 to 70 mL / 100 g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​68 to 78 m2 / g, more preferably an STSA surface area of ​​71 to 73 m2 / g, preferably a compressed oil absorption number of 58 to 69 mL / 100 g, more preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably volatiles of 2.0 to 2.6% by weight,more preferably volatiles of 2.2 to 2.4% by weight, preferably a transmittance at 425 nm in toluene greater than 40%, more preferably a transmittance at 425 nm in toluene greater than 56%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, Petition 870250076402, dated 08 / 28 / 2025, p. 119 / 136 6 / 9 surface area STSA is measured in accordance with ASTM D6556-21, with volatiles measured at 950°C for 7 min, as described in the descriptive report, and transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 in relation to toluene; and / or (III) carbon black having: a BET surface area of ​​80 to 96 m2 / g, preferably a BET surface area of ​​89 to 92 m2 / g, and a compressed oil absorption number of 60 to 69 mL / 100 g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g,preferably a surface area of ​​79 to 87 m² / g (STSA), more preferably a surface area of ​​82 to 84 m² / g (STSA), preferably volatiles of 2.2 to 2.9% by weight, more preferably volatiles of 2.5 to 2.7% by weight (STSA), preferably a transmittance at 425 nm in toluene greater than 40%, more preferably a transmittance at 425 nm in toluene greater than 62%, wherein the surface area of ​​the compressed oil (BET) is measured in accordance with ASTM D6556-21, the absorption number of compressed oil is measured in accordance with ASTM D3493-20 using paraffinic oil, the surface area of ​​the STSA is measured in accordance with ASTM D6556-21, the volatiles are measured at 950°C for 7 min, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 in relation to toluene; and / or (IV) carbon black having: BET surface area of ​​120 to 138 m2 / g, preferably BET surface area of ​​127 to 130 m2 / g, and Petition 870250076402, dated 08 / 28 / 2025,page. 120 / 136 7 / 9 a compressed oil absorption number of 58 to 69 mL / 100 g, preferably a compressed oil absorption number of 62 to 64 mL / 100 g, preferably a STSA surface area of ​​82 to 95 m² / g, more preferably a STSA surface area of ​​87 to 89 m² / g, preferably volatiles of 2.6 to 3.2% by weight, more preferably volatiles of 2.8 to 3.0% by weight, preferably a transmittance at 425 nm in toluene greater than 60%, more preferably a transmittance at 425 nm in toluene greater than 80%, wherein the BET surface area is measured in accordance with ASTM D6556-21, the compressed oil absorption number is measured in accordance with ASTM D3493-20 using paraffinic oil, the STSA surface area is Measurement in accordance with ASTM D6556-21, with volatiles measured at 950°C for 7 min, as described in the descriptive report.and the transmittance at 425 nm in toluene is measured in accordance with ASTM D 1618-18 with respect to toluene; and / or (V) carbon black having: a BET surface area of ​​82 to 95 m2 / g, preferably a BET surface area of ​​86 to 89 m2 / g, and a compressed oil absorption number of 59 to 70 mL / 100 g, preferably a compressed oil absorption number of 63 to 65 mL / 100 g, preferably an STSA surface area of ​​70 to 82 m2 / g, more preferably an STSA surface area of ​​76 to 78 m2 / g, preferably volatiles of 1.8 to 2.4% by weight, more preferably volatiles of 2.0 to 2.2% by weight, Petition 870250076402, dated 28 / 08 / 2025, p. 121 / 136 8 / 9 preferably a transmittance at 425 nm in toluene greater than 60%, more preferably a transmittance at 425 nm in toluene greater than 80%, and the BET surface area is measured according to ASTM D6556-21, the compressed oil absorption number is measured according to ASTM D3493-20 using paraffinic oil,The STSA surface area is measured according to ASTM D6556-21, with volatiles measured at 950°C for 7 minutes, as described in the descriptive report, and the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 with respect to toluene.

12. Composition, characterized in that it comprises: (A) an elastomeric polymeric material; and (B) carbon black obtained as defined in any one of claims 1 to 10.

13. Article, characterized in that it is made of, or comprises, the composition as defined in claim 12.

14. Use of a feedstock containing particulate carbon, characterized by the fact that it is for the manufacture of carbon black in an entrained flow reactor.

15. Method for adjusting the cooling position in an entrained flow reactor for the production of carbon black from a feedstock containing particulate carbon, characterized in that it comprises: I) injecting a feedstock containing particulate carbon into a hot gas stream of an entrained flow reactor, the hot gas stream having a temperature of at least 800°C, II) quenching the hot gas stream that makes up the carbon black produced, III) measuring the transmittance of the carbon black produced, Petition 870250076402, dated 08 / 28 / 2025, p. 122 / 136 9 / 9 III) adjust the cooling position in the entrained flow reactor until the transmittance of the carbon black produced is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured in accordance with ASTM D 161818 relative to toluene.Petition 870250076402, dated 08 / 28 / 2025, pp. 123 / 136.

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