Carbon black derived from particulate feedstock

Abstract

The invention relates to a method for producing carbon black in an entrained-flow reactor by using a particulate carbonaceous feedstock.

Description

TECHNICAL FIELD

[0001] The present invention relates to a process for producing carbon black in a gas flow bed reactor by using a particulate carbonaceous feedstock. BACKGROUND

[0002] The production of carbon black requires the pyrolysis or thermal decomposition of a carbonaceous feedstock in a reaction chamber at a temperature of, for example, 800°C (e.g. in the temperature range between 1 100°C and 2 000°C). These high temperatures are obtained by combustion of a mixture comprising an oxygen-containing gas and a combustion fuel (i.e. a fuel). The carbon black (CB) entrained in the gas (hot gas stream) exiting the reaction chamber is then cooled in a quenching operation and then collected by any suitable method commonly used in the art.

[0003] Carbon black has many uses, for example as a reinforcing agent or filler for the rubber and tire industry. In addition, the use of carbon black in other fields, for example as a colorant for copying machines and copying toner, has also increased. Various applications of carbon black require a wide variety of carbon black properties (e.g. particle size, structure, yield, surface area and tinting).

[0004] The formation of carbon black can be divided into different process steps, including the increase of the temperature of the feedstock to a pyrolysis temperature, the pyrolysis of the feedstock into unsaturated species (e.g. acetylene and aromatic hydrocarbon-containing intermediates), nucleation, surface growth and agglomeration.

[0005] In the prior art, the feedstock used for the production of carbon black in a gas flow bed reactor (e.g. a furnace reactor) is limited to liquid carbonaceous feedstocks. Liquid carbonaceous feedstocks are, for example, liquid hydrocarbons, such as oils similar to pyrolysis oils derived from a steam cracker or a fluidized catalytic cracker.

[0006] Upon injection of the liquid carbonaceous feedstock into the carbon black reactor, the feedstock is immediately vaporized and carbon black is formed. Compared to liquid carbonaceous feedstocks, particulate carbonaceous feedstocks are much slower in converting into gaseous components, and therefore it is difficult to achieve an ideal pyrolysis of particulate carbonaceous feedstocks.

[0007] As an alternative method, particulate carbonaceous feedstocks, for example from tires, can be pyrolyzed in a pyrolysis reactor. At low temperatures, for example at 500°C, a liquid fraction, a gaseous fraction and a solid fraction are obtained. The liquid fraction can then be used for the production of new or virgin carbon black (nCB) in a gas flow bed reactor (e.g. a furnace reactor).

[0008] US 2002 / 0117388 A1 relates to the pyrolysis of waste rubber materials, including old tires. The aim of US 2002 / 0117388 A1 is to recover components from the waste rubber materials, for example carbon black. After pyrolysis, carbon black can be recovered from the pyrolysis gas (recovered carbon black (rCB)).

[0009] However, the solids yield from pyrolysis at low temperatures is low, requiring subsequent manufacturing processes to obtain carbon black from the liquid fraction of the pyrolysis. Furthermore, the coke and ash content of the carbon black recovered after pyrolysis is unsatisfactory.

[0010] Therefore, a new method for producing carbon black should be developed that utilizes granular carbonaceous feedstock. Surprisingly, granular carbonaceous feedstock has been found to be usable in fluidized bed reactors, where the hot gas flow temperature is at least 800°C. Summary of the Invention

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

[0012] In addition, carbon black produced according to the method of the present invention is provided, as well as compositions comprising (A) an elastomeric polymer material and (B) carbon black obtained according to the present invention, and articles made from or containing compositions of the present invention are provided.

[0013] In addition, carbon black is provided, wherein (I) the carbon black has the following properties: BET surface area of ​​80 m² 2 / g to 90m 2 / g, with a preferred BET surface area of ​​85m² 2 / g to 88m 2 / g, and a compression oil absorption value of 58mL / 100g to 69mL / 100g, preferably 61mL / 100g to 64mL / 100g, and preferably an STSA surface area of ​​72m². 2 / g to 82m 2 / g, more preferably STSA surface area is 76m² 2 / g to 79m 2 / g, preferably volatile matter of 2.1% to 2.7% by weight, more preferably volatile matter of 2.3% to 2.5% by weight, preferably transmittance at 425 nm in toluene greater than 50%, more preferably transmittance at 425 nm in toluene greater than 77%, wherein the BET surface area is measured according to ASTM D6556-21, the compression oil absorption value is measured using paraffin oil according to ASTM D3493-20, the STSA surface area is measured according to ASTM D6556-21, wherein volatile matter is measured at 950°C for 7 minutes as described in the specification, and the transmittance at 425 nm in toluene is measured relative to toluene according to ASTM D 1618-18; and / or (II) carbon black has the following properties: BET surface area of ​​70m²2 / g to 85 m2 / g 2 / g, preferably a BET surface area of 77 m 2 / g to 79 m2 / g 2 / g, and a compressed oil absorption of 59 mL / 100g to 70 mL / 100g, preferably a compressed oil absorption of 63 mL / 100g to 65 mL / 100g, preferably a STSA surface area of 68 m 2 / g to 78 m2 / g 2 / g, more preferably a STSA surface area of 71 m 2 / g to 73 m2 / g 2 / g, preferably a compressed oil absorption of 58 mL / 100g to 69 mL / 100g, more preferably a compressed oil absorption of 63 mL / 100g to 65 mL / 100g, preferably volatiles of 2.0 wt% to 2.6 wt%, more preferably volatiles of 2.2 wt% to 2.4 wt%, preferably a transmittance in toluene at 425 nm of greater than 40%, more preferably a transmittance in toluene at 425 nm of greater than 56%, wherein the BET surface area is measured according to ASTM D6556-21, the compressed oil absorption is measured according to ASTM D3493-20 using paraffinic oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to the description at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D1618-18 relative to toluene; and / or (III) the carbon black has the following properties: a BET surface area of 80 m 2 / g to 96 m2 / g 2 / g, preferably a BET surface area of 89 m 2 / g to 92 m2 / g 2 / g, and a compressed oil absorption of 60 mL / 100g to 69 mL / 100g, preferably a compressed oil absorption of 63 mL / 100g to 65 mL / 100g, preferably a STSA surface area of 79 m 2 / g to 87 m2 / g 2 / g, more preferably a STSA surface area of 82 m 2 / g to 84 m2 / g 2 / g, preferably volatile matter of 2.2% to 2.9% by weight, more preferably volatile matter of 2.5% to 2.7% by weight, preferably transmittance at 425 nm in toluene greater than 40%, more preferably transmittance at 425 nm in toluene greater than 62%, wherein the BET surface area is measured according to ASTM D6556-21, the compression oil absorption value is measured using paraffin oil according to ASTM D3493-20, the STSA surface area is measured according to ASTM D6556-21, wherein volatile matter is measured at 950°C for 7 minutes as described in the specification, and the transmittance at 425 nm in toluene is measured relative to toluene according to ASTM D 1618-18; and / or (IV) carbon black has the following properties: BET surface area of ​​120m² 2 / g to 138m 2 / g, with a preferred BET surface area of ​​127m² 2 / g to 130m 2 / g, and a compression oil absorption value of 58mL / 100g to 69mL / 100g, preferably 62mL / 100g to 64mL / 100g, and preferably an STSA surface area of ​​82m². 2 / g to 95m 2 / g, more preferably STSA surface area is 87m² 2 / g to 89m 2 / g, preferably volatile matter of 2.6% to 3.2% by weight, more preferably volatile matter of 2.8% to 3.0% by weight, preferably transmittance at 425 nm in toluene greater than 60%, more preferably transmittance at 425 nm in toluene greater than 80%, wherein the BET surface area is measured according to ASTM D6556-21, the compression oil absorption value is measured using paraffin oil according to ASTM D3493-20, the STSA surface area is measured according to ASTM D6556-21, wherein volatile matter is measured at 950°C for 7 minutes as described in the specification, and the transmittance at 425 nm in toluene is measured relative to toluene according to ASTM D 1618-18; and / or (V) carbon black has the following properties: BET surface area of ​​82m 2 / g to 95m 2 / g, with a preferred BET surface area of ​​86m² 2 / g to 89m 2 / g, and a compression oil absorption value of 59mL / 100g to 70mL / 100g, preferably 63mL / 100g to 65mL / 100g, and preferably an STSA surface area of ​​70m². 2 / g to 82m 2 / g, more preferably STSA surface area is 76m² 2 / g to 78m 2 / g, preferably the volatiles are 1.8 wt.-% to 2.4 wt.-%, more preferably the volatiles are 2.0 wt.-% to 2.2 wt.-%, preferably the transmittance in toluene at 425 nm is more than 60 %, more preferably the transmittance in toluene at 425 nm is more than 80 %, wherein the BET surface area is measured according to ASTM D6556-21, the compressive oil absorption is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to the description at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene.

[0014] Furthermore, the particulate carbonaceous feedstock is used for manufacturing carbon black in an entrained flow reactor.

[0015] Furthermore, a method for adjusting the quenching position in an entrained flow reactor for producing carbon black from a particulate carbonaceous feedstock is provided, the method comprising: I) injecting the particulate carbonaceous feedstock into a hot gas stream of an entrained flow reactor, wherein the temperature of the hot gas stream is at least 800 °C, II) quenching the hot gas stream comprising the produced carbon black, II) measuring the transmittance of the produced carbon black, III) adjusting the quenching position in the entrained flow reactor until the transmittance of the produced carbon black is at least 20 %, preferably at least 30 %, more preferably at least 40 %, still more preferably at least 60 %, most preferably at least 80 %, wherein the transmittance in toluene at 425 nm is measured according to ASTM D1618-18 relative to toluene. BRIEF DESCRIPTION OF DRAWINGS

[0016] Figure 1 : Furnace reactor cross section

[0017] Figure 2 : Feed mixing device comprising a nozzle

[0018] Figure 3 : Laval-nozzle for a feed mixing device

[0019] Figure 4 : Depolymerization pipe for a feed mixing device

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

[0021] It must be noted that, as used herein, the singular articles "a", "an" and "the" can be interpreted to cover both singularly and plurally referenced forms, 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 so on.

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

[0023] The expression "feedstock" refers to the raw material used for the production of carbon black. According to the present application, a particulate feedstock is used for the production of carbon black. The expression or abbreviation feedstock as used in the present application refers to a particulate carbon-containing feedstock.

[0024] The expression "hot gas stream" refers to the carrier gas in an entrained flow reactor, such as a furnace reactor, which heats the reaction mixture, including the particulate carbon-containing feedstock, 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 refers to a material consisting essentially of, for example, greater than 80 wt.%, or greater than 90 wt.%, or greater than 95 wt.% carbon, based on the total weight thereof, produced by pyrolysis or radical-driven abstraction of non-carbon atoms in a carbon-containing feedstock. Different industrial processes for the production of carbon black are known, such as the furnace process, the gas black process, the acetylene black process, the thermal black process or the lamp black process. The production of carbon black is per se well known in the art, for example as outlined in J.-B. Donnet et al., Carbon Black: Science and Technology, 2ndEdition, and is therefore not described in detail herein.

[0026] The reaction volume of the reactor is the volume of the reactor between the location where the particulate carbon-containing feedstock is injected and the quenching location.

[0027] The present application relates to a process for the production of carbon black from a particulate carbon-containing feedstock in an entrained flow reactor having a flow channel along a longitudinal axis of the center of the reactor, the process comprising: (a) providing a hot gas stream, (b) providing a particulate carbon-containing feedstock, and (d) injecting the particulate carbon-containing feedstock into the hot gas stream to form carbon black, wherein the temperature of the hot gas stream is at least 800 °C.

[0028] Without being bound by theory, it is generally believed that the heating rate of a particulate carbon-containing feedstock is lower compared to a liquid carbon-containing feedstock, and therefore the particulate carbon-containing feedstock needs to be injected into the hot gas stream of the entrained flow reactor at a suitable temperature of 800 °C or even higher. For example, the temperature of the hot gas stream is 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, at least 1600 °C. The minimum temperature required can be determined by measuring the transmittance of the produced carbon black. If the transmittance is low, the temperature of the hot gas stream can be increased.

[0029] The hot gas stream can be obtained by electric preheating, plasma heating, and combustion of a fuel and an oxygen-containing gas. The hot gas stream can be provided by (a1) supplying the fuel and the oxygen-containing gas into a combustion chamber of the reactor, (b2) combusting the fuel in the combustion chamber to produce the hot gas stream.

[0030] Thus, the present application can relate to a process for producing carbon black from a particulate carbonaceous feedstock in an entrained-flow reactor having a flow passage along a longitudinal axis of the center of the reactor, the process comprising: (a) supplying a fuel and an oxygen-containing gas into a combustion chamber of the reactor, (b) combusting the fuel in the combustion chamber to produce a hot combustion gas, (d) injecting the particulate carbonaceous feedstock into the hot gas stream to form carbon black, wherein the temperature of the hot combustion gas is at least 800°C.

[0031] The particulate carbonaceous feedstock can comprise inert compounds, coke, C, H containing compounds, and / or carbon black, preferably carbon black and C, H containing compounds. The particulate carbonaceous feedstock is particulate, typically agglomerated particulate. In contrast, liquid carbonaceous feedstock means that the feedstock is liquid at 20°C and 1 atm. Preferably, the process for producing carbon black does not use a liquid carbonaceous feedstock to produce carbon black.

[0032] Typically, all of the feedstock used to produce carbon black is particulate carbonaceous feedstock.

[0033] The particulate feedstock can comprise up to 10 wt% oil (extender oil). For example, rubber particles typically comprise up to 10 wt% oil (extender oil). The oil or extender oil is typically a fatty oil or an aromatic oil.

[0034] The particulate carbonaceous feedstock is a feedstock suitable for producing carbon black (i.e. new carbon black). Thus, the particulate carbonaceous feedstock comprises a material that can be pyrolyzed.

[0035] The C, H containing compound (hydrocarbon compound) can be used to produce carbon black (i.e. new carbon black (nCB) or virgin carbon black (vCB)). The C, H containing compound means a compound that comprises both C and H. For example, the C, H containing compound is a hydrocarbon compound that can comprise a heteroatom (e.g. O or S).

[0036] The particulate carbonaceous feedstock can comprise 10 wt% to 100 wt% of the C, H containing compound, preferably 20 wt% to 99 wt% of the C, H containing compound, more preferably 30 wt% to 90 wt% of the C, H containing compound, most preferably 40 wt% to 70 wt% of the C, H containing compound, based on the total weight of the particulate carbonaceous feedstock.

[0037] The particulate carbonaceous feedstock can comprise inert compounds, which can comprise metals, metal compounds, silicon, silicon dioxide. The metal can be zinc, silicon, calcium, aluminium, and / or iron.

[0038] Based on the total weight of the granular carbon-containing raw material, the granular carbon-containing raw material may contain 1% to 40% by weight of inert compound, preferably 3% to 30% by weight of inert compound, more preferably 4% to 20% by weight of inert compound, and most preferably 5% to 15% by weight of inert compound.

[0039] The particulate carbon-containing feedstock may also include carbon black, i.e., recycled carbon black. This carbon black is commonly found in tires and is therefore recyclable. Based on the total weight of the particulate carbon-containing feedstock, it should contain 1% to 70% by weight of carbon black, preferably 5% to 60% by weight, more preferably 10% to 50% by weight, and most preferably 15% to 40% by weight. Alternatively, the particulate carbon-containing feedstock may not contain recycled carbon black.

[0040] In this document, recycled carbon black refers to carbon black that can be recovered during the process. In other words, it refers to carbon black present in the raw materials, not carbon black produced in the process of this invention.

[0041] C and H compounds are, for example, rubber, plastics, and / or biomass-based materials. Particulate carbon-containing raw materials are preferably provided in granular form (i.e., carbon-containing granular raw materials). Therefore, granular carbon-containing raw materials can include or be rubber granules, plastic granules, and / or biomass-based granules. Thus, granular carbon-containing raw materials can be granular rubber raw materials, granular plastic raw materials, and / or granular biomass-based raw materials. Preferably, the granular carbon-containing raw materials include rubber granules, wherein the rubber granules include carbon black.

[0042] By measuring the C14 content in the raw materials ( 14 C content (radiocarbon dating) can distinguish between biomass-based and fossil-based feedstocks. Compared to biomass-based feedstocks, fossil-based feedstocks have a higher relative abundance of C14 atoms to C12 atoms (C14 to C12 ratio). 14 C / 12 The C ratio is lower. Therefore, fossil-based raw materials refer to raw materials in which the relative amount of C14 atoms to C12 atoms is lower than the relative amount of naturally occurring (or bio-based) C14 atoms to C12 atoms.

[0043] Preferably, based on the total weight of the granular carbon-containing raw material, the content of granular biomass-based raw material in the granular carbon-containing raw material is 20% to 100% by weight, for example, 40% to 100% by weight, 50% to 99% by weight, 60% to 95% by weight, or 60% to 80% by weight.

[0044] Preferably, the content of the particulate plastic feedstock in the particulate carbonaceous feedstock is 20 wt% to 100 wt%, such as 40 wt% to 100 wt%, 50 wt% to 99 wt%, 60 wt% to 95 wt%, or 80 wt% to 90 wt%, based on the total weight of the particulate carbonaceous feedstock.

[0045] Preferably, the content of the particulate plastic feedstock in the particulate carbonaceous feedstock is 20 wt% to 100 wt%, such as 40 wt% to 100 wt%, 50 wt% to 99 wt%, 60 wt% to 95 wt%, or 80 wt% to 90 wt%, based on the total weight of the particulate carbonaceous feedstock.

[0046] The particulate biomass-based carbon black feedstock can include plant-based feedstock, preferably non-edible plant-based feedstock and / or waste plant-based feedstock. As used herein, the term “non-edible” refers to material that is not suitable for human consumption. The term “waste” refers to material that is discarded or disposed of because it is unsuitable or no longer suitable for its intended purpose, such as after use.

[0047] The particulate biomass-based carbon black feedstock can include wood, grass, cellulose, hemicellulose, lignin, and / or natural rubber.

[0048] As used herein, the term “wood” refers to the porous and 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, spruce, larch, juniper, ash, hornbeam, birch, alder, beech, oak, pine, chestnut, mulberry, or mixtures thereof. Suitable examples of grass include, but are not limited to, cereal grasses, such as corn, wheat, rice, barley, or millet; bamboo and native grasses of grasslands, as well as species planted in lawns and pastures. Suitable examples of lignin can include, but are not limited to, lignin removed by the Kraft process and lignosulfonate.

[0049] The rubber particles can include natural rubber and / or synthetic rubber. The particulate carbonaceous feedstock can include carbon black-containing rubber particles. Natural rubber can be derived from rubber trees (Helvea brasiliensis), guayule, and dandelions. The rubber particles or particulate carbonaceous feedstock can be derived from tires, cable sheaths, tubes, conveyor belts, shoe soles, hoses, or mixtures thereof.

[0050] The synthetic rubber can include styrene butadiene rubber, such as emulsion polymerized styrene butadiene rubber (ESBR) and solution polymerized styrene butadiene rubber (SSBR), polybutadiene, polyisoprene, ethylene propylene terpolymer rubber (EPDM), ethylene propylene rubber (EPM), butyl rubber, halogenated butyl rubber, chlorinated polyethylene, chlorosulfonated polyethylene, nitrile rubber, hydrogenated nitrile rubber, polychloroprene, acrylate rubber, ethylene vinyl acetate rubber, ethylene acrylic acid rubber, epichlorohydrin rubber, silicone rubber, fluorosilicone rubber, fluorocarbon rubber, or a mixture or combination of any of the foregoing.

[0051] The plastic particles or plastic particulate feedstock can be any plastic known in the art. For example, acrylic resins (such as polyacrylic acid or polymethyl methacrylate), polyesters (such as polyethylene terephthalate or polyethylene glycol), polyurethanes (such as derived from toluene diisocyanate (TDI) or methylene diphenyl diisocyanate), polyolefins (such as polypropylene, polyethylene or polystyrene). In general, thermoplastic and thermoset plastics can be used.

[0052] The plastic particles are preferably from waste material from households. For example, plastic bags, plastic containers, plastic packaging, and the like.

[0053] The feedstock is provided in particulate form. This can be achieved by grinding to the desired particle or grain size. For example, tyres can be ground to obtain particulate rubber particles as the feedstock.

[0054] It is desirable that at least 50 wt.%, preferably at least 60 wt.%, more preferably at least 70 wt.%, most preferably at least 80 wt.% of the particulate carbonaceous feedstock has a particle size of 125 pm to 2 mm, preferably 125 pm to 1 mm, more preferably 250 pm to 1 mm, most preferably 500 pm to 1000 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0055] It is desirable that at least 70 wt.%, preferably at least 80 wt.%, more preferably at least 90 wt.%, most preferably at least 98 wt.% of the particulate carbonaceous feedstock has a particle size of less than 2 mm, preferably less than 1 mm, more preferably less than 500 pm, most preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0056] It is desirable that at least 70 wt.%, preferably at least 80 wt.%, more preferably at least 90 wt.%, most preferably at least 98 wt.% of the particulate carbonaceous feedstock has a particle size of less than 500 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0057] It is desired that at least 70 wt.-%, preferably at least 80 wt.-%, more preferably at least 90 wt.-%, most preferably at least 98 wt.-% of the particulate carbonaceous feedstock have a particle size of less than 1 mm, wherein the particle size is measured according to ASTM D 1511 -12(2017).

[0058] It is desired that at least 70 wt.-%, preferably at least 80 wt.-%, more preferably at least 90 wt.-%, most preferably at least 98 wt.-% of the particulate carbonaceous feedstock have a particle size of less than 2 mm, preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511 -12(2017).

[0059] It is desired that less than 1 wt.-%, preferably at least 0.5 wt.-%, more preferably less than 0.1 wt.-%, most preferably less than 0.01 wt.-% of the particulate carbonaceous feedstock have a particle size of more than 2 mm, preferably more than 1 mm, more preferably more than 500 pm, most preferably more than 250 pm, wherein the particle size is measured according to ASTM D 1511 -12(2017).

[0060] It is particularly preferred that the particulate carbonaceous feedstock has a particle size of less than 2 mm, preferably less than 1 mm, more preferably less than 500 pm, most preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511 -12(2017).

[0061] The particle size of the particulate carbonaceous feedstock can be controlled by classifying the particulate carbonaceous feedstock prior to injecting it into the reactor. It is therefore preferred that the particulate carbonaceous feedstock is classified prior to injecting it into the reactor or prior to injecting it into the mixing feed unit.

[0062] The classification can be performed by any means known in the art, such as sieving or other classification. The classification can be performed using a vibrating sieve, a rotating sieve, a cyclone, an elutriation classifier, an air jet sieve and / or a dynamic air classifier. Any combination of the above can be used. The classification can be used to obtain the maximum or minimum desired particle size as described in the present specification.

[0063] The particle size of the particulate carbonaceous feedstock can be controlled by sieving the particulate carbonaceous feedstock prior to injecting it into the reactor. Sieve sizes as described in ASTM D 1511 -12(2017) can be used. For example, sieves having a mesh size of 2000 pm, 1000 pm, 500 pm, 250 pm or 125 pm, preferably 500 pm, 250 pm or 125 pm can be used. Furthermore, the sieves can have a pore size that retains particles having a size of more than 2000 pm, more than 1000 pm, more than 500 pm, more than 250 pm or more than 125 pm, preferably more than 500 pm, more than 250 pm or more than 125 pm.

[0064] No more than 10 wt.%, preferably no more than 5 wt.%, more preferably no more than 4 wt.%, most preferably no more than 2 wt.% of the particulate carbonaceous feedstock should have a particle size greater than 4 mm, preferably greater than 2 mm, more preferably greater than 1 mm, most preferably greater than 0.5 mm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0065] No more than 10 wt.%, preferably no more than 5 wt.%, more preferably no more than 4 wt.%, most preferably no more than 2 wt.% of the particulate carbonaceous feedstock should have a particle size less than 150 pm, preferably less than 125 pm, more preferably less than 110 pm, most preferably less than 100 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0066] No more than 10 wt.%, preferably no more than 5 wt.%, more preferably no more than 4 wt.%, most preferably no more than 2 wt.% of the particulate carbonaceous feedstock should have a particle size less than 150 pm, preferably less than 125 pm, more preferably less than 110 pm, most preferably less than 100 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0067] The particle size distribution of the particulate carbonaceous feedstock can be measured according to ASTM D 1511-12 (2017) and: (a) 1 wt.% to 0 to 10 wt.%, preferably 1 wt.% to 8 wt.%, more preferably 1 wt.% to 5 wt.%, most preferably 1 wt.% to 3 wt.% of the particulate carbonaceous feedstock is retained by the No. 10 sieve, and / or (b) 1 wt.% to 25 wt.%, preferably 2 wt.% to 20 wt.%, more preferably 4 wt.% to 15 wt.%, most preferably 5 wt.% to 12 wt.% of the particulate carbonaceous feedstock is retained by the No. 18 sieve, and / or (c) 10 wt.% to 80 wt.%, preferably 15 wt.% to 70 wt.%, more preferably 20 wt.% to 60 wt.%, most preferably 25 wt.% to 55 wt.% of the particulate carbonaceous feedstock is retained by the No. 35 sieve, and / or (d) 5 wt.% to 70 wt.%, preferably 10 wt.% to 60 wt.%, more preferably 15 wt.% to 50 wt.%, most preferably 20 wt.% to 45 wt.% of the particulate carbonaceous feedstock is retained by the No. 60 sieve, and / or (e) 1 wt.% to 80 wt.%, preferably 7 wt.% to 70 wt.%, more preferably 5 wt.% to 60 wt.%, most preferably 7 wt.% to 50 wt.% of the particulate carbonaceous feedstock is retained by the No. 120 sieve, and / or (f) the bottom receiving pan contains less than 4 wt.%, preferably less than 3 wt.%, more preferably 0 to 2 wt.%, most preferably 0.01 wt.% to 1 wt.% of the particulate carbonaceous feedstock. It is desirable to select the desired ranges independently for each sieve.

[0068] The 50% cumulative particle size by weight of the particulate carbon-containing feedstock should be from 100 pm to 4 mm, preferably from 100 pm to 3 mm, more preferably from 100 pm to 2 mm, most preferably from 100 pm to 500 pm, wherein the 50% cumulative particle size by weight is measured according to ASTM D 1511-12 (2017). The 50% cumulative particle size by weight can be determined by interpolation using standard techniques known in the art. It is particularly preferred that the 50% cumulative particle size by weight is determined by interpolation using a Rosin-Rammler-Sperling-Bennett distribution (RRSB distribution).

[0069] The weight average particle size Dw50 of the particulate carbon-containing feedstock can be from 100 pm to 4 mm, preferably from 100 pm to 3 mm, more preferably from 100 pm to 2 mm, most preferably from 100 pm to 500 pm, wherein the weight average particle size Dw50 is measured according to ASTM D 1511-12 (2017).

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

[0071] The particle size distribution Dw90 of the particulate carbon-containing feedstock can be from 400 pm to 4 mm, preferably from 500 pm to 3 mm, more preferably from 600 pm to 2 mm, most preferably from 700 pm to 500 pm, wherein the particle size distribution Dw90 is measured according to ASTM D 1511-12 (2017).

[0072] The particle size distribution span (Dw90-Dw10) / Dw50 of the particulate carbon-containing feedstock can be 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 according to ASTM D 1511-12 (2017).

[0073] The Dw50, Dw10 and Dw90 can be determined by interpolation using standard techniques known in the art. It is particularly preferred that the Dw50, Dw10 and Dw90 are determined by interpolation using a Rosin-Rammler-Sperling-Bennett distribution (RRSB distribution).

[0074] The particle or grain size has an effect on the heating rate of the feedstock in the reactor. Smaller particles or grains have a higher specific surface area and therefore a higher heating rate. A fast heating rate is beneficial so that the granular feedstock can evaporate and then pyrolyze. It can be considered that pyrolysis is significantly faster than the evaporation of the granular feedstock. The heating rate can also be increased by a higher hot gas stream temperature.

[0075] The carbon black produced according to the present application, for example including rCB, and / or the granular carbonaceous feedstock can have a pMC (percentage of modern carbon) of 1 % or more, for example 2% or more, or 5% or more, or 7% or more, or 10% or more, or 12% or more, or 15% or more, or 17% or more, or 20% or more, or 22% or more, or 25% or more, or 27% or more, or 30% or more, or 32% or more, or 35% or more, or 37% or more, or 40% or more, or 42% or more, or 45% or more, or 47% or more, or 50% or more, or 52% or more, or 55% or more, or 57% or more, or 60% or more, or 62% or more, 65% or more, or 67% or more, or 70% or more, or 72% or more, or 75% or more, or 77% or more, or 80% or more, or 82% or more, or 85% or more, or 87% or more, or 90% or more, or 92% or more, or 95% or more, or 97% or more, or 99% or more, as measured according to ASTM D6866-20 Method B (AMS). For each sample, the ratio of d13C to d13C of the oxalic acid II standard (NIST-4990C) is calculated and compared to the measured value of the oxalic acid II standard (NIST-4990C). The measured value (pMC) is corrected by using the d13C measured by isotope ratio mass spectrometry (IRMS). The carbon black of the present application can have a pMC (percentage of modern carbon) of 5% or more, preferably 10% or more, particularly preferably 15% or more, more preferably 50% or more, still more preferably 85% or more, most preferably 90% or more, as measured according to ASTM D6866-20 Method B (AMS). The carbon black of the present application can have a pMC (percentage of modern carbon) of 100% as measured according to ASTM D6866-20 Method B (AMS). 14 C / 13 The ratio of d13C to d13C of the oxalic acid II standard (NIST-4990C) is calculated and compared to the measured value of the oxalic acid II standard (NIST-4990C). The measured value (pMC) is corrected by using the d13C measured by isotope ratio mass spectrometry (IRMS). The carbon black of the present application can have a pMC (percentage of modern carbon) of 5% or more, preferably 10% or more, particularly preferably 15% or more, more preferably 50% or more, still more preferably 85% or more, most preferably 90% or more, as measured according to ASTM D6866-20 Method B (AMS). The carbon black of the present application can have a pMC (percentage of modern carbon) of 100% as measured according to ASTM D6866-20 Method B (AMS).

[0076] The obtained carbon black typically includes recycled carbon black and new carbon black. Recycled carbon black can typically be obtained if the granular carbonaceous feedstock comprises carbon black. New carbon black is obtained by pyrolysis, i.e. the process of the present application.

[0077] The mass flow of the feedstock should be adjusted so that the feedstock can be heated uniformly. The particulate carbon-containing feedstock should be injected into the reactor with a mass flow of 2 kg / h to 50 kg / h per 130 L of the reaction volume of the reactor, preferably 5 kg / h to 40 kg / h per 130 L of the reaction volume of the reactor, more preferably 8 kg / h to 30 kg / h per 130 L of the reaction volume of the reactor, most preferably 10 kg / h to 20 kg / h per 130 L of the reaction volume of the reactor.

[0078] The fuel can comprise a gaseous or liquid hydrocarbon, preferably natural gas, fuel oil or H2.

[0079] Hydrogen can be used as a carrier gas for the production of carbon black and / or as a fuel. Preferably, hydrogen is used as a carrier gas for the production of carbon black and as a fuel. Hydrogen will be used as a carrier gas if it is in molar excess in the combustion mixture relative to oxygen. Thus, hydrogen should be present in the hot combustion gas and the hot reaction mixture.

[0080] The temperature of the hot gas stream should be 900 °C to 3500 °C, preferably 950 °C to 3000 °C, more preferably 1000 °C to 2000 °C, most preferably 1200 °C to 1900 °C.

[0081] The hot gas stream can be obtained by electrical preheating, plasma heating and combustion of a fuel and an oxygen-containing gas. The combustion of the fuel and the oxygen-containing gas is preferably carried out in a furnace reactor. However, as mentioned above, other methods can also be possible which are able to provide the required temperature of the hot gas stream.

[0082] The entrained-flow reactor can be a furnace reactor. The furnace reactor can have a flow channel along the central longitudinal axis of the reactor. The reactor usually comprises, from upstream to downstream (flow direction), a combustion chamber, a choke and a tunnel comprising a quenching device. These components define a flow channel for the hot gas stream, e.g. hot combustion gas, along the central longitudinal axis of the reactor. Thus, these components should be fluidically connected, in particular along the central longitudinal axis of the reactor.

[0083] A tubular duct can be connected to the combustion chamber for supplying the oxygen-containing gas required for the combustion of the fuel (or combustion fuel). The tubular duct can also be placed along the central longitudinal axis of the reactor so that the supply of the oxygen-containing gas takes place along the flow channel described above. Furthermore, the reactor can comprise a fuel injection device for injecting the fuel into the combustion chamber.

[0084] Usually, a fuel lance is used for supplying the fuel into the combustion chamber. The combustion chamber can be connected to the tubular duct in a direction from downstream to upstream so that the 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, which is covered with a gastight, e.g. metallic, cover. The material forming the refractory and the outer lining can be materials common in the art, such as castable refractory with an alumina (AI2O3) content of 70% - 32 cm, with a melting point of about 1870 °C. In addition, refractory bricks such as RUBY SR (sold by Harrison-Walker Refractories, Pittsburgh, PA) can be used, which have an alumina content of 84.5 %, a chromia (Cr2O3) content of 9.8 %, and a melting point of about 2050 °C. The shell or lining is preferably formed of carbon steel, except for any piping in contact with hot process air. In these areas, the piping is made of "316 stainless steel".

[0086] The combustion chamber is preferably designed as a cylinder in size. Contraction sections (throat sections) can be provided downstream of the combustion chamber. The contraction sections have a conical passage and converge in the upstream to downstream direction. Preferably, these contraction sections are in the form of a truncated conical passage. The combustion chamber can also be conical in the downstream to upstream direction. Thus, the combustion chamber can comprise a region which tapers towards the reaction chamber and / or towards the tubular pipe.

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

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

[0089] The oxygen-containing gas and the fuel can be preheated electrically or using a heat exchanger.

[0090] Water has an influence on the surface properties of the produced carbon black. Thus, the amount of oxygen-containing gas, such as O2, in the combustion mixture can be used to control the water content in the hot combustion mixture and / or the hot reaction mixture, and thus preferably the surface properties of the produced carbon black.

[0091] The passage is connected to the combustion chamber such that the hot combustion gases obtained in the combustion chamber can flow into the passage. The passage can be placed along the central longitudinal axis of the reactor. The diameter of the reaction chamber can be higher than the diameter of the contraction section of the combustion chamber, such that the hot combustion gases can expand. The expansion section is preferably designed as a cylinder in size and communicates with the combustion chamber, preferably with the contraction section (throat section) of the combustion chamber.

[0092] The particulate carbonaceous feedstock can be injected into the combustion chamber, the throat section and / or the tunnel of the furnace reactor. Typically, the particulate carbonaceous feedstock is injected into the throat section (converging section).

[0093] If the particulate carbonaceous feedstock is injected into, for example, the combustion chamber, the particulate carbonaceous feedstock or the carrier gas comprising the feedstock should have the required pressure. This means that the pressure of the particulate carbonaceous feedstock or the carrier gas comprising the feedstock should be higher than the pressure in the combustion chamber. Therefore, a suitable feed mixing device configured to operate under pressurized conditions should be used.

[0094] The particulate carbonaceous feedstock should be injected through a plurality of inlets, preferably radially and perpendicular to the central longitudinal axis of the reactor.

[0095] The concentration of O2in the hot gas stream should be less than 5 vol.%, preferably less than 4 vol.%, more preferably 0.01 vol.% to 3 vol.%, most preferably 0.1 vol.% to 2 vol.%.

[0096] The obtained carbon black typically comprises recycled carbon black and fresh carbon black.

[0097] The particulate carbonaceous feedstock can be injected into the reactor by means for injecting the feedstock. The means for injecting the feedstock can comprise a plurality of nozzles or lances, which are preferably arranged circumferentially with respect to the central longitudinal axis. The circumferential arrangement further improves the uniformity of the carbon black, as the feedstock for the carbon black can be mixed homogeneously with the hot gas stream. The particulate carbonaceous feedstock can be introduced by various means for injecting the feedstock.

[0098] For example, axially extending feedstock lances and radially extending feedstock injectors can be implemented, the nozzles of which are capable of producing various conical sprays (e.g. 15, 30, 45 and 60 degree conical spray angles).

[0099] In order to produce the desired carbon black properties, the radially extending feedstock injectors can be equipped with shut off valves, such that the feedstock is introduced only through certain feedstock injectors, or the flow rate of the feedstock in the injectors is varied.

[0100] The means for injecting the feedstock are preferably connected to the feed mixing device. It is desirable that the feed mixing device provides a plurality of feedstock inlets. However, it is also possible to use a plurality of feed mixing devices.

[0101] The tunnel can further comprise means for injecting a quenching medium along the central longitudinal axis of the reactor into the flow tunnel, which means are located at a subsequent position with respect to the flow direction for injecting the carbon black feedstock. Alternatively, the quenching means can be a quenching boiler or a heat exchanger.

[0102] The tunnel can comprise means for injecting quenching medium along the central longitudinal axis of the reactor to the flow channel. The means for injecting quenching medium is located at a subsequent position relative to the flow direction of the means for injecting carbon black precursor. The quenching medium is typically H2O.

[0103] The distance between the precursor injection means and the means for injecting quenching medium (first means for injecting quenching medium) can be between 150 mm and 80000 mm, preferably between 900 mm and 50000 mm, more preferably between 1500 mm and 30000 mm, most preferably between 2500 mm and 20000 mm.

[0104] The means for injecting quenching medium can extend into the tunnel. For example, a cooling fluid pipe or a plurality of radial cooling fluid pipes can be used. The quenching medium, for example a cooling liquid such as water, can be sprayed within the tunnel to stop the carbon black reaction at the appropriate time and location.

[0105] The reactor can further comprise a tubular pipe for supplying an oxygen-containing gas to the combustion chamber. The oxygen-containing gas (O2-containing gas or O2-containing gas mixture) can be air, oxygen-enriched air, other oxygen-containing gas and / or pure oxygen. The tubular pipe can thus be connected with the combustion chamber such that the oxygen-containing gas is able to flow through the tubular pipe in the combustion chamber. The tubular pipe can be placed along the central longitudinal axis of the reactor. Desirably, the central longitudinal axis of the tubular pipe is coaxial with the central longitudinal axis of the reactor. The tubular pipe can thus be placed coaxially along the central longitudinal axis of the reactor. The weight % of oxygen present in the oxygen-containing gas should be between 20 wt% and 100 wt%, preferably between 50 wt% and 99 wt%, more preferably between 60 wt% and 95 wt%, most preferably between 70 wt% and 90 wt%, wherein the wt% is based on the total weight of the oxygen-containing gas.

[0106] The tubular pipe can have a cylindrical shape which extends along the central longitudinal axis of the reactor without bends.

[0107] The tubular pipe for supplying the oxygen-containing gas can have an inner diameter between 5 cm and 3 m, for example between 10 cm and 3 m, between 20 cm and 3 m, between 9 cm and 2.5 m, between 13 cm and 1.5 m, between 0.1 m and 2 m, between 20 cm and 1 m, between 30 cm and 1.5 m, between 15 cm and 60 cm or between 15 cm and 90 cm.

[0108] The fuel injection means for introducing any suitable combustion fuel (e.g. natural gas, fuel oil or other gaseous or liquid hydrocarbons, preferably natural gas, fuel oil or H2) can be configured in different ways. For example, the injection means can be provided 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 pipes provided circumferentially with respect to the central longitudinal axis of the tubular conduit, such that the injection angle of the fuel is substantially perpendicular to the flow direction of the oxygen-containing gas.

[0109] However, in addition to the fuel lance, a plurality of fuel injection means can be provided. For example, at the end of the tubular conduit, additional fuel injection means are provided rotationally symmetrically with respect to the central longitudinal axis of the tubular conduit.

[0110] The supply amount of oxygen-containing gas is typically in excess with respect to the amount of oxygen required for complete combustion of the fuel, and / or wherein the supply amount of oxygen-containing gas is such that the k value is in the range of 0.01 to 10, preferably 0.1 to 5, more preferably 0.5 to 2, most preferably 0.7 to 1. Wherein the k value is defined as the ratio of the stoichiometric O2 amount required for complete stoichiometric combustion of the fuel to the supplied O2 amount.

[0111] The flow rates of fuel and oxygen-containing gas can be adjusted to produce high temperatures, typically close to the stoichiometric ratio. The ratio must be adjusted to prevent the refractory material from melting. The oxygen-containing flow rate ranges quite widely, for example, from a low flow rate of about 1000 Nm 3 / h to a high flow rate of about 100 kNm 3 / h, such as 1000 Nm 3 / h to 100 kNm 3 / h, 1000 Nm 3 / h to 10 kNm 3 / h, 2000 Nm 3 / h to 3000 Nm 3 / h or 1000 Nm 3 / h to 2000 Nm 3 / h. However, the present application is not limited to these ranges; higher air flow rates are required for larger reactors, while lower air flow rates are required for smaller reactors.

[0112] The desired temperature of the hot gas stream can also be achieved by heating the gas stream by plasma. The gas stream can be preheated as described above.

[0113] A plasma torch can provide the plasma for the above heating. A design of a plasma torch is described in WO 1993 / 012633 Al. However, any means known in the art for generating a plasma can be used. The plasma can be formed by a plasma carrier gas, which is heated by an electric arc burning between electrodes. High temperatures of 2500 °C to 20000 °C are reached in the plasma zone, in which the plasma treatment can be achieved. The plasma carrier gas can be oxygen or hydrogen. Hydrogen is particularly preferred as plasma carrier gas.

[0114] A microwave plasma can also provide the plasma for the above treatment. For example, a microwave generator can be used, which provides microwave radiation inside the reaction chamber. Microwave radiation of 1 GHz to 300 GHz can be used. Alternatively, a radio frequency power source (RF generator) can be used to generate the plasma.

[0115] The residence time between the time of injection of the particulate carbonaceous feedstock into the reactor and the time of quenching of the product mixture should be 150 milliseconds to 4 seconds, preferably 200 milliseconds to 3 seconds, more preferably 250 milliseconds to 2 seconds, most preferably 250 milliseconds to 1 second. The residence time of the particulate carbonaceous feedstock refers to the time of evaporation and pyrolysis of the particulate carbonaceous feedstock. The quenching of the product mixture stops the pyrolysis of the particulate carbonaceous feedstock. The heating rate of the particulate carbonaceous feedstock is lower compared to liquid feedstocks, so evaporation and pyrolysis of the particulate carbonaceous feedstock usually requires more time.

[0116] The residence time of the particulate carbonaceous feedstock should be 150 milliseconds to 4 seconds, preferably 200 milliseconds to 3 seconds, more preferably 250 milliseconds to 2 seconds, most preferably 250 milliseconds to 1 second, wherein the residence time is calculated according to equation (1);

[0117]

[0118] where t r is the residence time, V is the reaction volume (in m 3 ), and Q is the volume flow (in m 3 *s -1 ).

[0119] The volume flow is the volume of fluid per second after injection of the particulate carbonaceous feedstock into the hot gas stream, preferably the volume of fluid is calculated according to the ideal gas law according to equation (2):

[0120]

[0122] where Q is the volume flow of the fluid (in m 3 *s -1 ), is the sum of the molar flow of the gaseous substances N2, CO2, CO, H2O, volatiles (in mol*s -1 ), R is the gas constant, i.e. 8.3145 J K -1 · mol -1 , T is the absolute temperature and P is the pressure. The pressure P can be measured in the reactor or 101 125 Pa can be used for the calculation. For and the amount of substance, all substances are considered to be gaseous (including the particulate carbonaceous feedstock). Volatiles are the volatiles of the particulate carbonaceous feedstock as 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 stream are calculated taking into account complete combustion of the fuel. For the remaining oxygen, it is assumed that one O2 leads to one H2O and one CO, the oxygen is considered to react with the carbonaceous material. The calculation takes into account the fluid after injection of the particulate carbonaceous feedstock in the hot gas stream (for the volume flow calculation) and the carbonaceous part of the feedstock is completely in the gas phase. Non-gaseous substances are not considered. Furthermore, pyrolysis of the carbonaceous part of the feedstock is not considered in the calculation. In the description, examples for the calculation are specified, which can be applied to the specific method of manufacturing carbon black.

[0123] The reaction volume of the reactor is the volume of the reactor between the location of injection of the particulate carbonaceous feedstock and the quenching location.

[0124] The residence time should be chosen in such a way that the C, H containing substances in the particulate carbonaceous feedstock are completely pyrolyzed.

[0125] The absolute temperature for the calculation of the volume flow can be measured directly in the reactor. In particular, the temperature is measured directly after injection of the feedstock into the reactor, for example 50 mm after injection of the feedstock. For example, the temperature can be measured with a pyrometer.

[0126] Alternatively, the absolute temperature T (for the calculation of the volume flow) can be calculated as follows. The calculation takes into account the combustion of the fuel in the furnace reactor. The process comprises the combustion of the fuel and the heating of the rubber particles to the reaction temperature. The residual oxygen of the combustion does not lead to complete combustion. Therefore, it can be assumed that CO and H2O with the same CO / H2O ratio will be formed depending on the C / H ratio of the feedstock.

[0127] The reaction temperature can be calculated by energy conservation:

[0128]

[0129] The mass flow of the fuel is denoted by m F , h F is the enthalpy difference between the temperature and pressure of the fuel at the entrance of the combustion chamber and the reference conditions of the fuel (T = 25 °C, P = 101 125 Pa), mA is the mass flow of inert substance, h A is the specific enthalpy difference of inert substance A between 25°C and 1.01325 bar and the conditions (TA, PA) of the inert substance introduced into the combustion chamber. The amount of inert substance is indicated by K. Inert substances are substances which do not change in an ideal process. These inert substances are, for example, nitrogen, carbon black, mineral substances and water. ΔH uF is the lower heating value of the fuel at a temperature of 25°C and a pressure of P = 101325 Pa. The enthalpy difference of the oxygen between the feed conditions and the reference conditions (T = 298.15 K, P = 101325 Pa) is indicated by , the mass flow of oxygen is indicated by . The specific enthalpy difference of the reaction products i between the reaction temperature T and the conditions at P = 101325 Pa and the reference conditions (T = 298.15 K, P = 101325 Pa) is indicated by h i . The corresponding mass flow is indicated by mp i , the lower heating value of the compound is indicated by H ui . If the particulate carbonaceous feedstock is transported to the reactor together with a gas stream, this gaseous mass flow is indicated by m T , the enthalpy difference between the conditions at the reactor inlet and the reference conditions (T = 25°C, P = 103125 Pa) of this mass flow is indicated by h T , H uT is the corresponding lower specific heating value. The heat loss is indicated by Q 损失 . The mass flow of the hydrocarbon fraction in the carbonaceous particles is indicated by m R . This can be calculated by means of the following equation:

[0130] m R = m s (1 - w - Konradson residual carbon)

[0131] The mass flow of the particulate carbonaceous feedstock is indicated by m s . The enthalpy difference of the hydrocarbons between the entry state and the reference state (T = 25°C, P = 101325 Pa) is indicated by h R , the corresponding lower heating value is H uR .

[0132] The lower heating value is determined in accordance with DIN 5499 and DIN 51857. If no gas is reported in DIN 51857, the heating value can be determined by means of the generated heat. These values are available in Properties of Gases and Liquids, NIST data book, etc. The lower heating value is based on the substance C x H y S z O wAssumption of complete oxidation and gaseous water as reaction product:

[0133]

[0134] where A is not an oxidizing species. A f is the substance A in form A of the combustion products. Thus, p = fe.

[0135] The heating value is:

[0136]

[0137] If the reference temperature for the heat generation is different from 298.15 K for the substance i, the heat can be calculated using the molar heat capacity:

[0138]

[0139] The molar heat capacities can be found using the same textbooks as Properties of Gases and Liquids, NIST data book.

[0140] If the fuel consists of more than one substance, the lower heating value can be determined by the composition:

[0141]

[0143] The mass fraction of component I is denoted by ξ i , the lower heating value of component i is denoted by ΔH u,i , and the number of substances in the fuel is denoted by P.

[0144] The enthalpy difference of a fuel containing more than one substance is calculated as follows:

[0145]

[0146] The average molecular weight of the fuel is determined by:

[0147]

[0148] M i is the molecular weight of substance i.

[0149] 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 by DIN 51900. According to the experimental results, the water content must be measured according to ASTM D4928-12 (2018) and the sulfur content and hydrogen content must be measured according to the methods described in the examples.

[0150] The enthalpy difference of the flue gas between T = 298.15 K and the flame temperature is determined as follows:

[0151]

[0152] The amount of substance in the product gas stream is denoted by N, the average molecular weight of the flue gas is denoted by M 气体 , the average molecular weight is determined by the following formula:

[0153]

[0155] The lower heating value of the inert substances in the product stream is set to 0 J / mol.

[0156] To determine the lower heating value of the hydrocarbon-containing substances in the particulate feedstock, the water content needs to be determined (ASTM D 4928-12 (2018)) and the Micro Conradson content needs to be determined according to ASTM D4530-15 (2020). In addition, the ultimate analysis of the particulate feedstock must be measured according to ASTM D 3176-15 (2016) and the gross heating value must be measured according to ASTM D 4809:2018.

[0157] The lower heating value of the particulate feedstock is calculated as follows:

[0158] H us = (H os - (w s + 9h s ) Δ vap h 水 ) 1 / (1-w)

[0159] In addition, the lower heating value of the Conradson residue can be determined using the same equation by measuring the gross heating value and the hydrogen content of the Conradson residue. The water content of the Conradson is 0. The lower heating value of the hydrocarbon-containing particles is determined by the following formula:

[0160] H uR = H us (1-w) - H u康拉逊残碳 Conradson residue) / (1-w- Conradson residue)

[0161] To determine the C / H ratio of the hydrocarbon fraction, it can be obtained from the ultimate analysis of the particulate feedstock and the ultimate analysis of the Conradson residue:

[0162]

[0163] The molar enthalpy difference of water can be determined by the following equation:

[0164]

[0165] For CO2, by the equation:

[0166]

[0167] For SO2,

[0168]

[0169] For N2,

[0170]

[0171] For O2,

[0172]

[0173] For CO,

[0174]

[0176] The low heating value of CO is

[0177] For gaseous rubber product:

[0178]

[0179] For granular rubber, we get

[0180] h 橡胶，s = 1960 J / kgK (T - 298.15 K)

[0181] Equation (19).

[0182] For Conradson carbon residue

[0183]

[0184] Exemplary calculations

[0185] Combustion of methane entering the combustion chamber at 3 bar and temperature T = 290 K

[0186] The standard volumetric flow of methane, taking into account a pressure of 101325 Pa and a temperature T = 273.15 K, is 13 Nm 3 / h (STP); the standard volumetric flow of nitrogen, taking into account a pressure of 101325 Pa and a temperature T = 273.15 K, is 118.5 Nm 331.5 Nm / h (STP); reference standard temperature T = 273.15 K and standard pressure P = 101325 Pa, standard oxygen flow is 31.5 Nm 3 / h (STP).

[0187] In the throat section, rubber particles are added to the system with a mass flow of 20 kg / h at a temperature of 20 °C and a pressure of 1 bar.

[0188] According to the DIN 51857 standard, the lower heating value of methane at T = 298.15 K and P = 101325 Pa is 802.6 MJ / kmol. In the Properties of Gases and Liquids, it is found that the heat capacity of methane is:

[0189] Cp(T) = 8.314462 * (4.568 - 8.975 / 10^3*T + 3,631 / 10^5*T^2 - 3.407 / 10^8*T^3 + 1.091 / 10^11*T^4)

[0190] Equation (22).

[0191] Thus, h is obtained by the following equation: f :

[0192]

[0193] The fuel feed temperature is denoted by T, in the example T = 290 K, and the reference temperature for the heating value is denoted by T0= 298.15 K.

[0194] The enthalpy difference between T = 298.15 K and the feed temperature for the inert gas nitrogen can be determined by equation (4). For oxygen, the enthalpy difference can be determined by equation (15).

[0195] Depending on the measured temperature of the shell, a heat loss will occur on the reactor shell, which can be calculated according to VDI The heat transfer should be calculated. The heat transfer should cover radiation and convection / free convection.

[0196] Calculation of compound mass flow in reaction zone

[0197] In equation (4), x = 1, y = 4, z = 0, w = 0 and p = 0. Thus, 13 Nm 3 / h methane is obtained. 13 Nm 3 / h CO2and 26 Nm 3 / h water. The remaining oxygen is determined from the total oxygen flow minus the oxygen flow in the form of CO2and H2O (if sulfur is present in the fuel, SO2). The conversion between the mass flow and the standard volume flow of gaseous substances is done by the following equation:

[0198]

[0199] T0 is 273.15 K, P 0 is 101325 Pa.

[0200] Thus, the residual oxygen flow is obtained:

[0201]

[0202] It is assumed that the residual oxygen is converted by hydrogen and carbon passing through the rubber part of the particle in the ratio of the atomic H / C ratio of the rubber part. Assuming an H / C ratio of 2, one H2O and one CO are obtained. Thus, a H2O flow of 5.5 Nm 3 / h must be added to the already calculated water flow, resulting in a total of 31.5 Nm 3 / h H2O and 5.5 Nm 3 / h CO. The rubber particles are transported to the reactor by 8 Nm 3 / h nitrogen.

[0203] The gas flows are converted into mass flows using the above equations, resulting in:

[0204]

[0205] The rubber mass flow in the gas phase is calculated by subtracting the inert mass from the total rubber particle flow and subtracting the mass flow of the combusted rubber.

[0206]

[0207] The Konarson residual carbon is considered an inert mass and can be calculated by the following equation.

[0208]

[0209] Calculation of heat loss

[0210] The heat flux can be calculated by the following equation.

[0211]

[0212] In the case of natural convection, a is calculated from the Nusselt number, which is a function of the Rayleigh number and the Prandtl number, Pr.

[0213]

[0214] Using the following equation

[0215]

[0216] The Rayleigh number is calculated by the following equation:

[0217]

[0218] Taking all this into account for energy conservation, the following equation is obtained:

[0219]

[0220] The outer surface area of the reactor is 15.9 m 2 . Thus, for the given example, 1629°C is obtained. The reaction volume is 0.162 m 3 . The volumetric flow of all materials, except for trace Conradson carbon (mConradson), is 1236 m 3 / h. Thus, the residence time is 0.38 seconds by the following equation:

[0221]

[0222] In the last equation, the reactor volume is denoted by V and the volumetric flow of all materials, except for Conradson carbon, is Q. In this example, all materials, except for Conradson carbon, are rubber, residual CO2, CO, H2O and N2.

[0223] Generally, the residence time is chosen in such a way that the C, H containing materials in the particulate carbon-containing feedstock are completely pyrolyzed.

[0224] The formation of carbon black is usually terminated by quenching of the hot gas stream. Thus, the method can further comprise (e) quenching the hot gas stream after injection according to step (d).

[0225] The transmittance can be indicative of whether the residence time of the feedstock is sufficient for complete pyrolysis of the C, H containing materials in the feedstock, for example. Thus, the hot gas stream should be quenched (e) when the transmittance of the carbon black obtained at 425 nm is at least 20%, preferably at least 30%, more preferably at least 40%, still more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured relative to toluene according to ASTM D 1618-18.

[0226] The transmittance of the carbon black produced at 425 nm can be measured and the quenching position can be adjusted until the transmittance of the carbon black produced at 425 nm is at least 20%, preferably at least 30%, more preferably at least 40%, still more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured relative to toluene according to ASTM D1618-18.

[0227] The quench position in the entrained flow reactor can be chosen such that the transmittance of the produced carbon black at 425 nm is at least 20 %, preferably at least 30 %, more preferably at least 40 %, still more preferably at least 60 %, most preferably at least 80 %, wherein the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 against toluene.

[0228] Further, a method of adjusting the quench position in an entrained flow reactor for producing carbon black from a particulate carbonaceous feedstock is provided, the method comprising: I) injecting the particulate carbonaceous feedstock into a hot gas stream of the entrained flow reactor, wherein the temperature of the hot gas stream is at least 800 °C, II) quenching the hot gas stream comprising the produced carbon black, II) measuring the transmittance of the produced carbon black, III) adjusting the quench position in the entrained flow reactor until the transmittance of the produced carbon black is at least 20 %, preferably at least 30 %, more preferably at least 40 %, still more preferably at least 60 %, most preferably at least 80 %, wherein the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 against toluene.

[0229] It is particularly preferred that the particulate carbonaceous feedstock is depolymerized prior to injection into the reactor. It is generally believed that the use of depolymerized particles can shorten the evaporation time.

[0230] It is therefore desirable that step (b) further comprises depolymerizing the particulate carbonaceous feedstock and that in step (d) the depolymerized particulate carbonaceous feedstock is injected into the hot gas stream to form the carbon black.

[0231] It is therefore desirable that step (b) further comprises depolymerizing the particulate carbonaceous feedstock and that in step (d) the depolymerized particulate carbonaceous feedstock is injected into the hot gas stream to form the carbon black.

[0232] Depolymerization can be achieved by (i) accelerating the particulate carbonaceous feedstock and / or (ii) applying a shear force, preferably using an extruder. Depolymerization can be carried out in (i) a feed mixing device, preferably comprising a nozzle, and / or (ii) an extruder. The feed mixing device is preferably a device according to the present application.

[0233] Acceleration of the particulate carbonaceous feedstock leads to depolymerization of the particles. For example, a carrier gas, such as N2or air, can be accelerated and the particles are injected into the accelerated carrier gas. In other words, depolymerization can be carried out by placing the particulate carbonaceous feedstock into a jet of carrier gas.

[0234] The deagglomeration can be performed in a (i) feed mixing device comprising a Laval nozzle.

[0235] The carrier gas and / or the particulate carbonaceous feedstock is preferably accelerated to more than 1 Ma, preferably 1.01 Ma to 1.7 Ma, more preferably 1.1 Ma to 1.6 Ma, most preferably 1.2 Ma to 1.5 Ma. Mach numbers (Ma) of more than 1 can be achieved using ejection nozzles such as Laval nozzles. Ma is the Mach number.

[0236] However, flow rates of 0.01 Ma to 3 Ma, preferably 0.1 Ma to 2 Ma, more preferably 0.2 Ma to 1.8 Ma, most preferably 0.3 Ma to less than 1 Ma are also desirable.

[0237] The deagglomeration can also be achieved by impact of the accelerated particulate carbonaceous feedstock with an object, such as two particulate carbonaceous feedstock particles, or by impact of a particle of the particulate carbonaceous feedstock with a surface, such as the inner surface of a deagglomeration pipe.

[0238] The deagglomerated particulate carbonaceous feedstock (or carrier gas comprising the deagglomerated particulate carbonaceous feedstock) 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 bar to 1.3 bar, most preferably 0.8 bar to 1.2 bar. As mentioned above, the pressure should be adjusted according to the injection position of the feedstock. For example, the pressure in the combustion chamber is higher than the pressure in the throat section, so the deagglomerated particulate carbonaceous feedstock or carrier gas comprising the deagglomerated particulate carbonaceous feedstock should be injected into the combustion chamber at a higher pressure.

[0239] The deagglomerated particulate carbonaceous feedstock can be contained in a carrier gas, which further comprises H2O and / or an additive. The H2O can prevent re-agglomeration of the particles in the carrier gas. Thus, the deagglomerated particulate carbonaceous feedstock should be contained in a carrier gas, and the carrier gas can further comprise 1 vol% to 10 vol% H2O, preferably 2 vol% to 8 vol% H2O, more preferably 3 vol% to 7 vol% H2O, based on the total volume of the carrier gas comprising the deagglomerated particulate carbonaceous feedstock.

[0240] The particulate carbonaceous feedstock and / or the deagglomerated carbonaceous feedstock is typically contained in a carrier gas.

[0241] Depolymerization can be performed in a feed mixing device for feeding particles to a reactor, the feed mixing device comprising: (i) a carrier gas channel extending through the feed mixing device, (ii) at least one carrier gas inlet in fluid connection with the carrier gas channel, (iii) at least one particle inlet, (iv) a mixing chamber in fluid connection with the at least one particle inlet and the carrier gas inlet; (v) a depolymerization conduit in fluid connection with the mixing chamber; (vi) at least one outlet for the carrier gas entraining particles that have been fed to the mixing chamber, wherein the at least one outlet is in fluid connection with the depolymerization conduit; and (vii) a device for accelerating the carrier gas stream and injecting the carrier gas stream into the mixing chamber.

[0242] The gas channel should extend along a longitudinal axis through the feed mixing device, preferably the at least one inlet, the mixing chamber, the depolymerization conduit and the outlet are aligned with the longitudinal axis.

[0243] The particle inlet should be configured to feed particles to the mixing chamber at an angle relative to the jet stream of carrier gas discharged into the mixing chamber, preferably perpendicular to the jet stream of carrier gas. However, for the present invention, the angle is not particularly limited.

[0244] The device for accelerating the carrier gas stream and injecting the carrier gas stream can comprise at least one jet nozzle (nozzle). The jet nozzle is configured to accelerate the carrier gas stream. This means that the position of the nozzle (or jet nozzle) is such that the nozzle converges in the flow direction, thereby accelerating the gas stream after leaving the nozzle and entering the mixing chamber. In other words, the device for accelerating the carrier gas stream and injecting the carrier gas stream preferably converges in the flow direction extending from the at least one carrier gas stream inlet towards the at least one outlet.

[0245] The jet nozzle can be a Laval nozzle. Such a Laval nozzle (or nozzle) can comprise (in the following order) a converging section, a throat and a diverging section. Typically, the converging section reduces the diameter of the nozzle, thereby accelerating the gas stream. The diverging section increases the diameter of this section. However, the increased diameter of the diverging section is still smaller than the diameter before the converging section. Thus, by comprising a converging section, a throat and a diverging section in the following order, the gas stream is accelerated.

[0246] The cross-sectional area at each point of the jet nozzle is typically circular or elliptical.

[0247] The jet nozzle can comprise a diverging section, the angle of the diverging section can be from 2° to 30°, preferably from 3° to 20°, more preferably from 4° to 15°, most preferably from 5° to 10°.

[0248] The injection nozzle can comprise a converging section, the maximum inner diameter of the converging section can be 5 mm to 50 mm, preferably 8 mm to 40 mm, more preferably 10 mm to 30 mm, most preferably 12 mm to 20 mm.

[0249] The minimum inner diameter of the converging section, the diverging section and / or the inner diameter of the throat can be 0.6 mm to 30 mm, preferably 1.2 mm to 18 mm, more preferably 1.9 mm to 12 mm, most preferably 3 mm to 9 mm.

[0250] The minimum inner diameter of the converging section, the diverging section and the inner diameter of the throat should be the same. In other words, the converging section, the throat and the diverging section are usually directly connected to each other.

[0251] The injection nozzle can comprise a diverging section, the maximum inner diameter of the diverging section can be 0.3 mm to 11 mm, preferably 0.5 mm to 7 mm, more preferably 0.9 mm to 5 mm, most preferably 1.1 mm to 4 mm.

[0252] The minimum inner diameter of the converging section should be greater than the maximum inner diameter of the converging section, preferably the difference between the maximum inner diameter of the converging section and the diverging section is 5 mm to 30 mm, preferably 8 mm to 20 mm, more preferably 9 mm to 18 min, most preferably 10 mm to 15 mm.

[0253] The maximum inner diameter of the converging section can be greater than the maximum inner diameter of the diverging section.

[0254] The distance between the device for acceleration and injection and the pipe with constant inner diameter can be 2 mm to 20 mm, preferably 2.5 mm to 15 mm, more preferably 3 mm to 10 mm, most preferably 3.5 mm to 7 mm. The specific distance between the above-mentioned components can improve the deagglomeration of the particles, since the injection flow directly flows into the deagglomeration pipe. Thus, turbulent flow can be avoided and the speed loss of the injection flow is minimized.

[0255] The device for acceleration and injection of the carrier gas (or the nozzle) can be positioned such that the device for acceleration and injection of the carrier gas protrudes into the cavity of the inlet funnel of the deagglomeration pipe.

[0256] The deagglomeration pipe usually comprises a pipe with constant inner diameter. In the pipe with constant inner diameter, the particles collide with each other or the particles collide with the wall of the pipe with constant inner diameter for further deagglomeration. The deagglomeration pipe can be configured as a diffuser.

[0257] The deagglomeration conduit can comprise from downstream to upstream an inlet funnel, a conduit with constant inner diameter and a diffuser nozzle diverging in the flow direction. The nozzle for diverging should continuously increase the inner diameter of the deagglomeration conduit. Thus, the carrier gas stream is not interrupted, avoiding turbulent flow. The angle of the diffuser nozzle can be from 1 ° to 30°, preferably from 2° to 20°, more preferably from 3° to 15°, most preferably from 4° to 8°. The angle of the inlet funnel can be from 20° to 80°, preferably from 30° to 75°, more preferably from 40° to 70°, most preferably from 50° to 65°.

[0258] The longitudinal axis of the deagglomeration conduit can be coaxial with the longitudinal axis of the feed mixing device. The coaxial arrangement improves the overall acceleration and deagglomeration.

[0259] The inner diameter of the conduit with constant inner diameter can be from 1 mm to 20 mm, preferably from 2 mm to 10 mm, more preferably from 3 mm to 7 mm, most preferably from 4 mm to 6 mm. The inner diameter has an influence on the deagglomeration. Thus, the diameter should be chosen depending on the specific particulate feedstock, preferably depending on the mass flow.

[0260] The maximum inner diameter of the diffuser nozzle is larger than the inner diameter of the conduit with constant inner diameter. The maximum inner diameter of the diffuser nozzle should be from 5 mm to 50 mm, preferably from 8 mm to 40 mm, more preferably from 10 mm to 30 mm, most preferably from 12 mm to 20 mm.

[0261] The converging section of the diffuser nozzle and the jet stream nozzle can have the same maximum inner diameter.

[0262] The maximum inner diameter of the diffuser nozzle can be from 5 mm to 50 mm, preferably from 8 mm to 40 mm, more preferably from 10 mm to 30 mm, most preferably from 12 mm to 20 mm.

[0263] The length of the conduit with constant inner diameter can be from 3 mm to 500 mm, preferably from 5 mm to 200 mm, more preferably from 10 mm to 50 mm, most preferably from 13 mm to 30 mm. The length of the conduit has a beneficial influence on the deagglomeration of the particles (particulate carbonaceous feedstock). A longer conduit usually leads to a better deagglomeration.

[0264] The length of the diffuser nozzle can be from 10 mm to 300 mm, preferably from 20 mm to 200 mm, more preferably from 25 mm to 150 mm, most preferably from 30 mm to 100 mm.

[0265] The inner diameter of the conduit with constant inner diameter should be larger than the maximum inner diameter of the outlet of the device for accelerating and injecting the carrier gas stream.

[0266] The device for accelerating and injecting the carrier gas stream, the mixing chamber and the deagglomeration conduit can be configured such that the carrier gas jet is discharged in the deagglomeration conduit.

[0267] The feed mixing device can further comprise at least one hopper upstream of the at least one particle inlet.

[0268] Upstream of the at least one particle inlet there is typically at least one screw conveyor, e.g. one screw conveyor. The screw conveyor should be configured to provide a constant amount of particles (or particulate carbon-containing feedstock) into the mixing chamber. Thus, the supply of particles can be controlled by the screw conveyor.

[0269] The particles for the feed mixing device are particulate carbon-containing feedstock and the reactor is typically a gas flow reactor for the production of carbon black.

[0270] The feed mixing device typically further comprises a pressure tank for the particles, wherein the pressure tank is in fluid connection with the at least one particle inlet, optionally with the at least one screw conveyor. Preferably, there are two pressure tanks, wherein the first pressure tank is connected to the second pressure tank. Both pressure tanks can be connected by a valve.

[0271] A reactor system can be provided, which comprises a gas flow reactor and a feed mixing device, wherein the feed mixing device is in fluid connection with the reactor. The feed mixing device should be connected to the multiple inlets of the reactor, preferably by lances.

[0272] The feed mixing device can be in fluid connection with a throat section, a combustion chamber and / or a channel upstream of a quench zone of a gas flow reactor. The reactor can be a gas flow reactor, preferably a furnace reactor.

[0273] A method for injecting a particulate material into a reactor can be provided, which method comprises the steps of (a) deagglomerating and entraining particles in a carrier gas stream, preferably by using a feed mixing device, and (b) injecting the carrier gas stream comprising the deagglomerated particles obtained in step (a) into the reactor.

[0274] The method can be a method for the production of carbon black, the particulate material is particulate carbon-containing feedstock and the reactor is a gas flow reactor, preferably a furnace reactor, for the production of carbon black.

[0275] The particulate carbon-containing feedstock can be injected into the gas flow reactor through multiple inlets, preferably through multiple lances.

[0276] The carrier gas stream can be accelerated and flow through the mixing chamber into the deagglomeration duct.

[0277] Deagglomeration can be achieved by accelerating the particles in the carrier gas stream and colliding the particles with the inner surface of the deagglomeration duct.

[0278] The carrier gas is typically accelerated to more than 1 Ma, preferably 1.01 Ma to 1.7 Ma, more preferably 1.1 Ma to 1.6 Ma, most preferably 1.2 Ma to 1.5 Ma.

[0279] The particles can be subjected to the carrier gas jet perpendicularly to the carrier gas jet.

[0280] The carrier gas stream comprising the depolymerized 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 bar to 1.3 bar, most preferably 0.8 bar to 1.2 bar.

[0281] The carrier gas can further comprise H2O and / or an additive. The content of H2O in the carrier gas can be 1 vol% to 10 vol%. H2O can prevent re-agglomeration of the particles.

[0282] A feed mixing device can be used to depolymerize the particles, preferably to depolymerize the particulate carbonaceous feedstock.

[0283] Furthermore, a carbon black produced according to the inventive process is provided. The carbon black can comprise a fresh carbon black as well as a recycled carbon black.

[0284] Carbon black is included in many polymeric compositions, for example, to modify their color, mechanical properties, electrical properties, and / or processing properties. For example, carbon black is typically added to rubber compositions used to make tires or parts thereof to impart electrical dissipative properties to the insulating matrix. At the same time, the carbon black additive influences mechanical and elastic properties, such as stiffness, abrasion resistance, and hysteresis, which properties greatly influence the performance of the resulting tire, for example, in terms of its rolling resistance and durability.

[0285] According to the present invention, a composition is provided comprising (A) an elastomeric polymeric material and (B) a carbon black obtained according to the present invention. It is worth noting that also articles derived from said composition can be used as raw materials.

[0286] The term "composition" as used herein refers to a material made up of a plurality of chemical substances or components. An "elastomeric polymeric material" is to be understood as a material consisting essentially of an elastomeric polymer. The term "polymer" is used herein in its common meaning in the art, referring to a macromolecular compound, i.e. a compound of relatively high molecular weight (e.g. above 500 Da), the structure of which comprises a number of repeating units (also referred to as "mers"), which are actually or conceptually derived from chemical substances of relatively low molecular weight. The term "elastomeric polymer" is used herein in its common meaning in the art, referring to a polymer having elasticity.

[0287] Elastomeric polymeric materials (or elastomeric polymeric materials) particularly suitable for the practice of the present application are elastomers such as rubber materials. The elastomeric polymeric material (A) according to the composition of the present application can comprise one or more rubbers. The terms "rubber", "rubber material" and "elastomer" can be used interchangeably throughout the present specification unless otherwise indicated. The rubbers that can be used according to the present application include those containing unsaturated olefins, i.e. diene-based rubber materials, as well as non-diene-based rubber materials. The term "diene-based rubber material" is intended to include natural rubber and synthetic rubber or mixtures thereof. The elastomeric polymeric material (a) can consist of synthetic rubber.

[0288] The elastomeric polymeric material (A) according to the composition of the present application can include natural rubber and / or synthetic rubber.

[0289] Natural rubber can be used in its unprocessed form and in various processed forms conventionally known in the rubber processing art. Natural rubber can be obtained, for example, from rubber trees (Helvea brasiliensis), guayule and dandelion. Thus, the elastomeric polymeric material (a) can include or consist of natural rubber.

[0290] Synthetic rubber can include styrene butadiene rubber such as emulsion polymerized styrene butadiene rubber (ESBR) and solution polymerized styrene butadiene rubber (SSBR), polybutadiene, polyisoprene, terpolymer ethylene propylene diene rubber (EPDM), ethylene propylene rubber (EPM), butyl rubber, halogenated butyl rubber, chlorinated polyethylene, chlorosulfonated polyethylene, nitrile rubber, hydrogenated nitrile rubber, polychloroprene, acrylate rubber, ethylene vinyl acetate rubber, ethylene acrylic acid rubber, epichlorohydrin rubber, silicone rubber, fluorosilicone rubber, fluorocarbon rubber or mixtures or combinations of any of the foregoing. According to the present application, synthetic rubber can also be obtained from renewable source materials. For example, polybutadiene can be produced from alcohols obtained by fermentation of plant biomass.

[0291] Suitable rubbers can also include functionalized rubbers and rubbers combined with silicon or tin. For example, the rubbers can be functionalized with amine, alkoxy, silyl, thiol, thioester, thioether, thioalkyl, mercapto, sulfide or combinations thereof and the like functional groups. The one or more functional groups can be primary, secondary or tertiary functional groups, can be located at one or both chain ends (e.g. alpha, omega functionalization), pendant from the polymer backbone and / or contained within the chain of the polymer backbone. The rubbers according to the present application can also be partially crosslinked. Thus, prior to use in the composition of the present application, a portion of the polymer chains of the rubber material can be crosslinked, with or without coupling agents.

[0292] The composition according to the present application can specifically be a curable composition, such as a vulcanizable rubber composition. The term "vulcanizable rubber composition" refers to a composition that optionally contains various other components commonly used in the rubber compounding art, which composition is curable by vulcanization to form a vulcanizate. Unless otherwise indicated, the terms "curable" and "vulcanizable" are used interchangeably in this specification and refer to the chemical reaction of crosslinking agents or vulcanizing agents to interconnect polymer chains. The curing reaction can be induced by any means known in the art, such as by light, moisture, heat, and / or addition of a crosslinking agent.

[0293] The elastomeric polymeric material (A) according to the present application can include natural rubber. According to the present application, the natural rubber can include natural rubber obtained from a mixture of rubber tree (Helvea brasiliensis), guayule, dandelion, or a combination of any of the foregoing. The natural rubber can include natural rubber obtained from guayule and / or dandelion. The elastomeric polymeric material (A) can include 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 of natural rubber. 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) can include 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 of natural rubber. The elastomeric polymeric material (A) can include natural rubber in any range between the lower and upper limits. For example, the elastomeric polymeric material (A) can include natural rubber in the range of 5 phr to 95 phr, such as 10 phr to 90 phr, or 20 phr to 80 phr, or 30 phr to 70 phr, or 40 phr to 60 phr. According to the present application, the elastomeric polymeric material (A) can consist of natural rubber.

[0294] The elastomeric polymeric material (A) according to the present application can include a synthetic rubber. According to the present application, the synthetic rubber can include a synthetic rubber obtained from a renewable source material. The renewable source material according to the present application can be an alcohol obtained by fermentation of plant biomass. For example, the synthetic rubber can include a polybutadiene obtained from an alcohol obtained by fermentation of plant biomass. The elastomeric polymeric material (A) can include 5 phr or more of synthetic rubber, for example 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 of synthetic rubber. 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) can include 100 phr or less of synthetic rubber, for example 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 70 phr or less, or 65 phr or less, or 60 phr or less of synthetic rubber. The elastomeric polymeric material (A) can include synthetic rubber in a range between the lower and upper limits. For example, the elastomeric polymeric material (A) can include synthetic rubber in a range of 5 phr to 95 phr, for example 10 phr to 90 phr, or 20 phr to 80 phr, or 30 phr to 70 phr, or 40 phr to 60 phr of natural rubber. According to the present application, the elastomeric polymeric material (A) can consist of synthetic rubber.

[0295] According to the present application, the elastomeric polymeric material (A) can comprise a mixture of natural rubber and synthetic rubber. The elastomeric polymeric material (A) can comprise 5 phr to 100 phr of natural rubber and 5 phr to 100 phr of synthetic rubber, for example 10 phr to 90 phr of natural rubber and 10 phr to 90 phr of synthetic rubber, or 20 phr to 80 phr of natural rubber and 20 phr to 80 phr of synthetic rubber, or 30 phr to 70 phr of natural rubber and 30 phr to 70 phr of synthetic rubber, or 40 phr to 60 phr of natural rubber and 40 phr to 60 phr of synthetic rubber, or 40 phr to 100 phr of natural rubber and 5 phr to 60 phr of synthetic rubber, or 50 phr to 95 phr of natural rubber and 5 phr to 50 phr of synthetic rubber, or 60 phr to 90 phr of natural rubber and 10 phr to 50 phr of synthetic rubber, or 5 phr to 40 phr of natural rubber and 60 phr to 100 phr of synthetic rubber or 10 phr to 20 of natural rubber and 80 phr to 90 phr of synthetic rubber. For example, the elastomeric polymeric material (A) can comprise 50 phr of natural rubber and 50 phr of synthetic rubber, or the elastomeric polymeric material (A) can comprise 5 phr of natural rubber and 95 phr of synthetic rubber.

[0296] The synthetic rubber according to the present application preferably comprises a mixture of emulsion polymerized styrene butadiene rubber (ESBR), polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a combination of any of the foregoing, more preferably polyisoprene and / or polybutadiene, still more preferably polybutadiene. The synthetic rubber according to the present application preferably comprises a mixture of emulsion polymerized styrene butadiene rubber (ESBR), polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a combination of any of the foregoing, more preferably polyisoprene and / or polybutadiene, still more preferably polybutadiene. The synthetic rubber can comprise a mixture of emulsion polymerized styrene butadiene rubber (ESBR), polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a combination of any of the foregoing, preferably polyisoprene or polybutadiene, more preferably polybutadiene. The synthetic rubber can comprise or consist of polybutadiene, polyisoprene, butyl rubber, halogenated butyl rubber, or a combination of any of the foregoing, preferably polyisoprene and / or polybutadiene, more preferably polybutadiene. The synthetic rubber can comprise or consist of polybutadiene, polyisoprene, halogenated butyl rubber, or a combination of any of the foregoing, preferably polyisoprene and / or polybutadiene, more preferably polybutadiene.

[0297] The carbon black produced can also be comminuted prior to addition to the composition. Thus, the composition can comprise powdered carbon black.

[0298] The composition can comprise from 3 phr to 200 phr of the carbon black (B) obtained according to the present application, preferably from 5 phr to 190 phr of the carbon black (B) obtained according to the present application, more preferably from 10 phr to 150 phr of the carbon black (B) obtained according to the present application, still more preferably from 20 phr to 130 phr of the carbon black (B) obtained according to the present application, most preferably from 30 phr to 100 phr of the carbon black (B) obtained according to the present application.

[0299] The composition can comprise one or more additives selected from vulcanizing agents, curing aids (such as primary and secondary vulcanization accelerators, activators and presulfurization inhibitors), processing additives (such as oils, waxes, resins, plasticizers, flexibilizers, rheology modifiers, pigments, peptizing agents, coupling agents, surfactants), biocides and antidegradants (such as heat or light stabilizers, antioxidants and antiozonants), metal oxides, metal hydroxides and fillers (such as silica, organosilica, carbon nanotubes, carbon fibers, graphite and metal fibers).

[0300] The composition of the present application can be obtained and processed by common elastomer processing techniques. The composition according to the present application can be obtained, for example, by combining and mixing the carbon black (B) of the present application and any optional ingredients, if used, with the elastomeric polymeric material (A), for example to disperse the carbon black (B) and any optional ingredients, if used, in the elastomeric polymeric material (A). The dispersion can be achieved by any means known in the art, for example by mixing, stirring, milling, kneading, ultrasonics, dissolver, shaker mixer, rotor-stator dispersion assembly or high pressure homogenizer or combinations thereof. For example, a laboratory mixer with intermeshing rotor geometry can be used. The dispersion can be carried out, for example, until the carbon black (B) is uniformly dispersed in the elastomeric polymeric material (A), resulting in a dispersion index greater than 95% or more, preferably 97% or more or greater than 99% (classification according to ASTM D 2663-88 test method B).

[0301] The preparation of the composition according to the present application can be carried out, for example, in a multi-step process: first, the carbon black (B) and optionally non-curing additives, if used, can be added simultaneously or sequentially to the elastomeric polymeric material (A). Then, the elastomeric polymeric material (A), the carbon black (B) and the additives, if used, can be mixed, typically at a temperature of from 40 °C to 160 °C, for a total mixing time of less than 10 minutes, for example in the range of from 2 minutes to 8 minutes. Subsequently, the obtained mixture can be mixed with one or more curing additives at a temperature of less than 115 °C for less than 5 minutes, typically less than 3 minutes, preferably about 2.5 minutes.

[0302] The process can further comprise steps such as extrusion or cooling the product to room temperature and storing for further processing. The process can also comprise a curing step, which can be performed for example by placing the composition under heat curing conditions (e.g. a temperature of 120°C to 200°C for 5 minutes to 3 hours). Curing can be performed in a curing press at a temperature of 140°C to 180°C for 5 minutes to 60 minutes under a pressure of 100 bar to 150 bar.

[0303] It will be appreciated that the composition according to the present application can be used for various technical applications requiring a polymer-based material having a carbon black filler, such as for imparting antistatic or conductive properties, color, mechanical reinforcement and / or low hysteresis properties. Mechanical properties of interest, especially for tire production, include tear resistance, resilience and hysteresis. The composition according to the present application provides a cured composition having good and beneficial mechanical properties, especially for tire production. Beneficial mechanical properties according to the present application are for example high tensile strength, high resilience and low hysteresis. The composition according to the present application provides a cured composition having mechanical properties comparable to rubber compositions comprising conventional carbon black.

[0304] The present application therefore also relates to an article, in particular a tire, made of or comprising the above-mentioned composition according to the present application. The tire according to the present application can comprise a tread, a carcass, a sidewall, an inner liner, an apex, a shoulder, a shoulder cap, a chafer and / or a bead filler, wherein at least one of the above is made of or comprises the composition according to the present application. Such tires include, for example but not limited to, truck tires, passenger car tires, off-the-road tires, aircraft tires, agricultural tires and bulldozer tires. The tire and / or tire components can also be used as rubber granules.

[0305] The tire can comprise a sidewall, wherein the sidewall is made of the composition according to the present application, wherein the composition preferably comprises: (A) 40 phr to 60 phr of natural rubber and 40 phr to 60 phr of synthetic rubber, preferably 50 phr to 60 phr of natural rubber and 40 phr 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, more preferably consists of, polybutadiene; and (B) 30 phr to 70 phr of carbon black, preferably 40 phr to 60 phr, the tire comprising a tread, a carcass, a sidewall, an inner liner, an apex, a shoulder, a shoulder cap, a chafer and / or a bead filler, wherein at least the carbon black, preferably 50 phr of carbon black.

[0306] The tire can comprise a carcass, wherein the carcass is made from a composition according to the present application, wherein the composition preferably comprises: (A) 40 phr to 80 phr of natural rubber and 20 phr to 60 phr of synthetic rubber, preferably 50 phr to 70 phr of natural rubber and 30 phr 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 emulsion polymerized styrene butadiene rubber (ESBR), more preferably 20 phr of polybutadiene and 20 phr of emulsion polymerized styrene butadiene rubber (ESBR); and (B) 5 phr to 70 phr of carbon black, preferably 40 phr to 60 phr of carbon black, more preferably 50 phr of carbon black.

[0307] The tire comprises a chafer, wherein the chafer is made from a composition according to the present application, wherein the composition preferably comprises: (A) 30 phr to 70 phr of natural rubber and 30 phr to 70 phr of synthetic rubber, preferably 40 phr to 60 phr of natural rubber and 40 phr 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 emulsion polymerized styrene butadiene rubber (ESBR), more preferably consists of emulsion polymerized styrene butadiene rubber (ESBR); and (B) 55 phr to 95 phr of carbon black, preferably 65 phr to 85 phr of carbon black, preferably 75 phr of carbon black.

[0308] The tire can comprise a bead filler and / or apex core, wherein the bead filler and / or apex core is made from a composition according to the present application, wherein the composition preferably comprises: (A) 80 phr to 100 phr of natural rubber, preferably 90 phr to 100 phr of natural rubber, more preferably 100 phr of natural rubber; and (B) 35 phr to 75 phr of carbon black, preferably 45 phr to 65 phr of carbon black, more preferably 55 phr of carbon black.

[0309] The tire can comprise an inner liner, wherein the inner liner is made from a composition according to the present application, wherein the composition preferably comprises (A) 80 phr to 100 phr of synthetic rubber, preferably 90 phr to 100 phr of synthetic rubber, more preferably 100 phr of synthetic rubber, wherein the synthetic rubber preferably comprises halogenated butyl rubber, more preferably consists of halogenated butyl rubber; and (B) 40 phr to 80 phr of carbon black, preferably 50 phr to 70 phr of carbon black, more preferably 60 phr of carbon black.

[0310] The tire can comprise a tread, preferably a truck tire, wherein the tread is made from a composition according to the present application, wherein the composition preferably comprises (A) 60 phr to 95 phr of natural rubber and 5 phr to 40 phr of synthetic rubber, preferably 70 phr to 85 phr of natural rubber and 15 phr 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, more preferably consists of, polybutadiene; and (B) 30 phr to 70 phr of carbon black, preferably 40 phr to 60 phr of carbon black, more preferably 50 phr of carbon black.

[0311] The tire can comprise a tread, preferably a passenger car tire, wherein the tread is made from a composition according to the present application, wherein the composition preferably comprises (A) 80 phr to 100 phr of synthetic rubber, preferably 90 phr to 100 ppr of synthetic rubber, more preferably 100 phr of synthetic rubber, wherein the synthetic rubber preferably comprises, more preferably consists of, solution styrene butadiene rubber (SSBR) and polybutadiene, more preferably 70 phr of solution styrene butadiene rubber (SSBR) and 30 phr of polybutadiene; and (B) 35 phr to 75 phr of carbon black, preferably 45 phr to 65 phr of carbon black, more preferably 55 phr of carbon black.

[0312] The tire can comprise a tread, preferably a passenger car tire, wherein the tread is made from a composition according to the present application, wherein the composition preferably comprises (A) 80 phr to 100 phr of synthetic rubber, preferably 90 phr to 100 ppr of synthetic rubber, more preferably 100 phr of synthetic rubber, wherein the synthetic rubber preferably comprises, more preferably consists of, solution styrene butadiene rubber (SSBR) and polybutadiene, more preferably 70 phr of solution styrene butadiene rubber (SSBR) and 30 phr of polybutadiene; and (B) 3 phr to 25 phr of carbon black, preferably 5 phr to 15 phr of carbon black, more preferably 5 phr of carbon black; and (C) 60 phr to 100 phr of silica, preferably 70 phr to 90 phr of silica, more preferably 80 phr of silica.

[0313] The tire can comprise a tread, preferably an off-the-road (OTR) tire, wherein the tread is made from a composition according to the present application, wherein the composition preferably comprises (A) 80 phr to 100 phr of natural rubber, preferably 90 phr to 100 ppr of natural rubber, more preferably 100 phr of natural rubber; and (B) 35 phr to 75 phr of carbon black, preferably 45 phr to 75 phr of carbon black, more preferably 55 phr of carbon black.

[0314] The article can be a cable jacket, a tube, a power belt, a conveyor belt, a roller cover, a shoe sole, a hose, a seal, a profile, a damping element, a coating, or a colored or printed article.

[0315] Furthermore, the article can be a conveyor belt, wherein the conveyor belt is made of a composition according to the present application, 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, more preferably consists of, polybutadiene; and (B) 30 to 70 phr of carbon black, preferably 40 to 60 phr, more preferably 50 phr of carbon black.

[0316] Furthermore, the present application relates to the use of the above-mentioned composition according to the present application for the production of a tire, preferably a pneumatic tire, a tire tread, a belt, a belt reinforcement, a carcass, a carcass reinforcement, a sidewall, an apex, a shoulder, a chafer, a chafer cover, a bead cover, a bead filler, a cable jacket, a tube, a drive belt, a conveyor belt, a roller cover, a shoe, a hose, a seal, a profile, a damping element, a coating or a colored or printed article.

[0317] Furthermore, the present application uses depolymerized particulate carbonaceous feedstock for the manufacture of carbon black in an entrained flow reactor.

[0318] The present application will now be described with reference to the accompanying drawings, which do not limit the scope and ambit of the present application. The description provided is purely by way of example and illustration. However, the specific features illustrated in the drawings can be used to further limit the scope and ambit of the present application and the claims.

[0319] In Figure 1The figure shows a furnace reactor (100) comprising a combustion chamber (101), a throat section (102), and a passage (103). The reactor has an inner liner (106) and an outer liner (105). The combustion chamber (101) includes a fuel injection device (101b) and an oxygen-containing gas device (101a). In the figure, oxygen-containing gas is injected tangentially or radially into the combustion chamber (101) through the oxygen-containing gas device (101a), and fuel is injected axially into the combustion chamber (101) through the fuel injection device (101b). Preferably, the oxygen-containing gas is preheated to the temperature described in the specification. The temperature of the hot gas flow can be adjusted by preheating the oxygen-containing gas. Alternatively, the fuel can be preheated. In the combustion chamber (101), the fuel burns in the presence of the oxygen-containing gas. After combustion, the temperature of the hot carrier gas is above 800°C to bring the particulate carbonaceous feedstock to the temperature required for pyrolysis. Particulate carbonaceous feedstock can be directly injected into the combustion chamber (101), the throat section (102), or the channel (103). Particulate carbonaceous feedstock can also be injected into, for example, the throat section (102) or the channel (103) in any combination of the above. The furnace reactor (100) includes multiple locations (104a, 104b, 104c, 104d) for quenching. A quenching medium, typically water, lowers the temperature of the hot gas stream (or product mixture), thereby terminating the reaction for carbon black formation. Therefore, the location of the quenching affects the residence time of the feedstock and the composition derived from it. This means that if the quenching location is further adjusted downstream of the reactor, the residence time will increase. For example, quenching at a location (104a) near the throat section (102) results in a shorter residence time, while quenching at a location (104c) downstream of the reactor results in a longer residence time. The reaction volume refers to the reactor volume between the feedstock injection and quenching locations. If the raw material is injected into the channel (103), the distance between the quenching position and the raw material injection is 4200 mm, and the channel diameter is 200 μm, then the resulting reaction volume is 132 L. As described in the specification, the feed rate of the particulate carbon-containing raw material should be adjusted according to the reaction volume. For this invention, the quenching position at the rear of the channel is particularly preferred to allow sufficient time for the particulate carbon-containing raw material to evaporate or pyrolyze.

[0320] Reference Figure 2 The diagram shows a feed mixing device (200) comprising a carrier gas inlet (204), a particle inlet (201), a device (207) for accelerating and injecting the carrier gas flow, a depolymerization conduit (209), a mixing chamber (206), and an outlet (210) for the carrier gas entrained with the particles. A carrier gas passage (212) is also present. Figure 2 As shown in the diagram, a carrier gas passage (212) extends longitudinally through the feed mixing device. Carrier gas (203) enters the feed mixing device (200) through a carrier gas inlet (204) and is accelerated in a device (207) for accelerating and injecting the carrier gas flow.Figure 2 In this process, the device (207) for accelerating and injecting the carrier gas flow is configured as a Laval nozzle. The Laval nozzle includes a converging region (207a) along the flow direction. The resulting carrier gas jet is injected into a mixing chamber (206). Particles, such as granular carbonaceous raw material (202), are injected vertically into the mixing chamber (206). Thus, particles are entrained in the accelerated carrier gas. The sudden acceleration of the particles leads to their deagglomeration. The accelerated carrier gas containing the particles is further injected into a 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), thereby achieving further deagglomeration. It is desirable to configure the device (207) for accelerating and injecting the carrier gas flow so that the carrier gas jet is injected directly into the deagglomeration conduit (209). Therefore, velocity loss can be minimized. The depolymerization conduit (209) typically comprises, from downstream to upstream (in the flow direction), an inlet funnel (209a), a conduit (209b) with a constant inner diameter, and a diffuser nozzle (209c) diverging in the flow direction. The inlet funnel (209a) also allows for optimal flow behavior into the conduit (209b) with a constant inner diameter. The diffuser nozzle diverging in the flow direction (209c) also facilitates flow behavior. The outlet (406) can be connected according to... Figure 1 Apparatus for injecting feedstock into the reactor. Preferably, a feed mixing device (200) supplies the depolymerized feedstock to multiple devices for injecting the feedstock into the reactor. It is further desirable that the feed mixing device (200) includes 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 feed mixing device (200) can operate at a pressure of, for example, 1.5 bar or 2 bar. Pressure tanks for the particles (e.g., granular carbonaceous feedstock) can be installed. Such pressure tanks are fluidly connected to the particle inlet (201) and preferably connected to the feed mixing device (200) via valves. Preferably, two pressure tanks are present, with a first pressure tank connected to a second pressure tank. Both pressure tanks can be connected via valves.

[0321] exist Figure 3 The image shows a Laval nozzle (300) for a feed mixing device (200). A carrier gas passage (306) extends along the longitudinal axis through the Laval nozzle (300). Carrier gas (304) enters the Laval nozzle (300) and is accelerated. Then, a carrier gas jet (305) exits the Laval nozzle (300). The Laval nozzle (300) includes a section (301) with a constant diameter, 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 speed exceeding 1 Ma.

[0322] In Figure 4 depolymerization pipe (400) for a feed mixing device (200) is shown. A carrier gas channel (407) extends along a longitudinal axis through the depolymerization pipe (400). The depolymerization pipe (400) comprises an inlet funnel (401), a pipe (402) with a constant inner diameter and a diffuser nozzle (403) that is dispersed in the flow direction (403a). Furthermore, an outlet (404) is shown, which can be connected to a device that injects depolymerized particles, such as depolymerized particulate carbonaceous particles (406) into a reactor.

[0323] In Figure 5 another feed mixing device (500) is shown. A carrier gas channel (506) is also shown in Figure 5 the feed mixing device. The feed mixing device (500) comprises an inlet (504) for a carrier gas (501), a mixing chamber (505), an inlet (502) for particles and an outlet (503). The carrier gas (501) enters the feed mixing device (500). The carrier gas (501) should have a desired velocity, such as below 1 Ma or between 2 m / s and 1 Ma or between 20 m / s and 200 m / s. Particles, such as particulate carbonaceous particles (202) are injected vertically into the mixing chamber (507). Thus, the particles are entrained in the accelerated carrier gas. The sudden acceleration of the particles leads to a depolymerization of the particles. The outlet (503) can be connected to a reactor. Similar to the feed mixing device (200), a screw conveyor and at least one pressure tank can be installed.

[0324] Furthermore, the present invention will be described in the following few aspects.

[0325] 1st aspect: A method for producing carbon black from a particulate carbonaceous feedstock in an entrained flow reactor having a flow passage along a longitudinal axis of the center of the reactor, the method comprising:

[0326] (a) providing a hot gas stream,

[0327] (b) providing a particulate carbonaceous feedstock, and

[0328] (d) injecting the particulate carbonaceous feedstock into the hot gas stream to form carbon black,

[0329] wherein the temperature of the hot gas stream is at least 800 °C.

[0330] 2nd aspect: The method according to the 1st aspect, wherein step (b) further comprises subjecting the particulate carbonaceous particles to a depolymerization, and in step (d) the depolymerized particulate carbonaceous feedstock is injected into the hot gas stream to form carbon black.

[0331] Aspect 3: A method for producing carbon black from a particulate carbon-containing feedstock in an entrained-flow reactor having a flow channel along a longitudinal axis of the center of the reactor, the method comprising:

[0332] (a) providing a hot gas stream,

[0333] (b) depolymerizing the particulate carbon-containing particles to provide a depolymerized particulate carbon-containing feedstock, and

[0334] (d) injecting the depolymerized particulate carbon-containing feedstock into the hot gas stream to form carbon black,

[0335] wherein the hot gas stream has a temperature of at least 800 °C.

[0336] Aspect 4: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock comprises inert compounds, coke, C,H-containing compounds, and / or carbon black, preferably ash and carbon black.

[0337] Aspect 5: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock further comprises inert compounds, the inert compounds comprising zinc, silicon, calcium, aluminum, and / or iron.

[0338] Aspect 6: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock comprises 1 to 40 wt.-% of inert compounds, preferably 3 to 30 wt.-% of inert compounds, more preferably 4 to 20 wt.-% of inert compounds, most preferably 5 to 15 wt.-% of inert compounds, based on the total weight of the particulate carbon-containing feedstock.

[0339] Aspect 7: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock further comprises carbon black, wherein the carbon black is present in the particulate carbon-containing feedstock in an amount of 1 to 70 wt.-%, preferably 2 to 50 wt.-%, more preferably 5 to 40 wt.-%, most preferably 10 to 30 wt.-%, based on the total weight of the particulate carbon-containing feedstock.

[0340] Aspect 8: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock comprises 10 to 100 wt.-% of C,H-containing compounds, preferably 20 to 99 wt.-% of C,H-containing compounds, more preferably 30 to 90 wt.-% of C,H-containing compounds, most preferably 40 to 70 wt.-% of C,H-containing compounds, based on the total weight of the particulate carbon-containing feedstock.

[0341] Aspect 9: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock comprises rubber particles, plastic particles, and / or biomass-based particles.

[0342] Aspect 10: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock comprises rubber particles, wherein the rubber particles comprise carbon black.

[0343] Aspect 11 : The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock comprises agglomerated feedstock.

[0344] Aspect 12: The method according to any one of the preceding aspects, wherein at least 50 wt.%, preferably at least 60 wt.%, more preferably at least 70 wt.%, most preferably at least 80 wt.% of the particulate carbon-containing feedstock has a particle size of 125 pm to 2 mm, preferably 125 pm to 1 mm, more preferably 250 pm to 1 mm, most preferably 500 pm to 1000 pm, wherein the particle size is measured according to ASTM D 1511 -12(2017).

[0345] Aspect 13: The method according to any one of the preceding aspects, wherein the particle size distribution of the particulate carbon-containing feedstock is measured according to ASTM D1511 -12(2017) and:

[0346] (a) the No. 10 sieve retains from 1 wt.% to 0 to 10 wt.%, preferably 1 wt.% to 8 wt.%, more preferably 1 wt.% to 5 wt.%, most preferably 1 wt.% to 3 wt.% of the particulate carbon-containing feedstock, and / or

[0347] (b) the No. 18 sieve retains from 1 wt.% to 25 wt.%, preferably 2 wt.% to 20 wt.%, more preferably 4 wt.% to 15 wt.%, most preferably 5 wt.% to 12 wt.% of the particulate carbon-containing feedstock, and / or

[0348] (c) the No. 35 sieve retains from 10 wt.% to 80 wt.%, preferably 15 wt.% to 70 wt.%, more preferably 20 wt.% to 60 wt.%, most preferably 25 wt.% to 55 wt.% of the particulate carbon-containing feedstock, and / or

[0349] (d) the No. 60 sieve retains from 5 wt.% to 70 wt.%, preferably 10 wt.% to 60 wt.%, more preferably 15 wt.% to 50 wt.%, most preferably 20 wt.% to 45 wt.% of the particulate carbon-containing feedstock, and / or

[0350] (e) the No. 120 sieve retains from 1 wt.% to 80 wt.%, preferably 7 wt.% to 70 wt.%, more preferably 5 wt.% to 60 wt.%, most preferably 7 wt.% to 50 wt.% of the particulate carbon-containing feedstock, and / or

[0351] (f) the bottom receiving tray contains less than 4 wt.%, preferably less than 3 wt.%, more preferably 0 to 2 wt.%, most preferably 0.01 wt.% to 1 wt.% of the particulate carbon-containing feedstock.

[0352] The 14th aspect: The method according to any one of the preceding aspects, wherein not more than 10 wt.-%, preferably not more than 5 wt.-%, more preferably not more than 4 wt.-%, most preferably not more than 2 wt.-% of the particulate carbon-containing feedstock have a particle size of more than 4 mm, preferably more than 2 mm, more preferably more than 1 mm, most preferably more than 0.5 mm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0353] The 15th aspect: The method according to any one of the preceding aspects, wherein not more than 10 wt.-%, preferably not more than 5 wt.-%, more preferably not more than 4 wt.-%, most preferably not more than 2 wt.-% of the particulate carbon-containing feedstock have a particle size of less than 150 pm, preferably less than 125 pm, more preferably less than 110 pm, most preferably less than 100 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0354] The 16th aspect: The method according to any one of the preceding aspects, wherein the 50 wt.-% cumulative particle size of the particulate carbon-containing feedstock is from 100 pm to 4 mm, preferably from 100 pm to 3 mm, more preferably from 100 pm to 2 mm, most preferably from 100 pm to 500 pm, wherein the 50 wt.-% cumulative particle size is measured according to ASTM D 1511-12 (2017).

[0355] The 17th aspect: The method according to any one of the preceding aspects, wherein the weight average particle size Dw50 of the particulate carbon-containing feedstock is from 100 pm to 4 mm, preferably from 100 pm to 3 mm, more preferably from 100 pm to 2 mm, most preferably from 100 pm to 500 pm, wherein the weight average particle size Dw50 is measured according to ASTM D 1511-12 (2017).

[0356] The 18th aspect: The method according to any one of the preceding aspects, wherein the particle size distribution Dw10 of the particulate carbon-containing feedstock is from 100 pm to 250 pm, preferably from 110 pm to 220 pm, more preferably from 120 pm to 210 pm, most preferably from 130 pm to 200 pm, wherein the particle size distribution Dw10 is measured according to ASTM D 1511-12 (2017).

[0357] The 19th aspect: The method according to any one of the preceding aspects, wherein the particle size distribution Dw90 of the particulate carbon-containing feedstock is from 400 pm to 4 mm, preferably from 500 pm to 3 mm, more preferably from 600 pm to 2 mm, most preferably from 700 pm to 500 pm, wherein the particle size distribution Dw90 is measured according to ASTM D 1511-12 (2017).

[0358] The 20th aspect: The method according to any one of the preceding aspects, wherein the particle size distribution span (Dw90-Dw10) / Dw50 of the particulate carbon- containing feedstock 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 distribution Dw10, Dw50 and Dw90 are measured according to ASTM D 1511-12 (2017).

[0359] The 21st aspect: The method according to any one of the preceding aspects, wherein the method for producing carbon black does not use a liquid carbon-containing feedstock for producing carbon black.

[0360] The 22nd aspect: The method according to any one of the preceding aspects, wherein the hot gas stream is obtained by electric preheating, plasma heating and combustion of the fuel and the oxygen-containing gas.

[0361] The 23rd aspect: The method according to any one of the preceding aspects, wherein the hot gas stream is provided by the following steps:

[0362] (a1) supplying the fuel and the oxygen-containing gas into a combustion chamber of the reactor,

[0363] (b2) combusting the fuel in the combustion chamber to produce the hot gas stream.

[0364] The 24th aspect: The method according to any one of the preceding aspects, wherein the entrained-flow reactor is a furnace reactor.

[0365] The 25th aspect: The method according to any one of the 22nd to 24th aspect, wherein the particulate carbon-containing feedstock is injected into the combustion chamber, the throat section and / or the passage of the furnace reactor, preferably into the throat section of the furnace reactor.

[0366] The 26th aspect: The method according to any one of the preceding aspects, wherein the temperature of the hot gas stream is from 900 °C to 3500 °C, preferably from 950 °C to 3000 °C, more preferably from 1000 °C to 2000 °C, most preferably from 1200 °C to 1900 °C.

[0367] The 27th aspect: The method according to any one of the 22nd to 26th aspect, wherein the oxygen-containing gas is preheated to a temperature between 200 °C and 1600 °C, preferably to a temperature between 350 °C and 1400 °C, more preferably to a temperature between 500 °C and 1200 °C, most preferably to a temperature between 450 °C and 950 °C.

[0368] The 28th aspect: The method according to any one of the 22nd to 27th aspect, wherein the fuel is preheated to a temperature between 50 °C and 750 °C, preferably to a temperature between 100 °C and 700 °C, more preferably to a temperature between 300 °C and 700 °C, most preferably to a temperature between 450 °C and 650 °C.

[0369] Aspect 29: The method according to any one of aspects 22 to 28, wherein the supplied oxygen-containing gas is air, oxygen-enriched air or oxygen.

[0370] Aspect 30: The method according to any one of aspects 22 to 29, wherein the fuel comprises a gaseous or liquid hydrocarbon, preferably natural gas, fuel oil or H2.

[0371] Aspect 31 : The method according to any one of aspects 22 to 30, wherein the amount of oxygen-containing gas supplied results in an excess of oxygen relative to the amount of oxygen required for complete combustion of the fuel, and / or wherein the amount of oxygen-containing gas is such that the k-value is in the range of 0.01 to 10, preferably 0.1 to 5, more preferably 0.5 to 2, most preferably 0.7 to below 1.

[0372] Aspect 32: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock is injected through a plurality of inlets, preferably inlets that are radial and perpendicular to the central longitudinal axis of the reactor.

[0373] Aspect 33: The method according to any one of the preceding aspects, wherein the concentration of O2 in the hot gas stream is less than 5 vol.%, preferably less than 4 vol.%, more preferably 0.01 to 3 vol.%, most preferably 0.1 to 2 vol.%.

[0374] Aspect 34: The method according to any one of the preceding aspects, wherein the obtained carbon black comprises recycled carbon black and fresh carbon black.

[0375] Aspect 35: The method according to any one of the preceding aspects, wherein the residence time is the time between injection of the particulate carbon-containing feedstock into the reactor and the time of quenching of the product mixture, the residence time being 150 milliseconds to 4 seconds, preferably 200 milliseconds to 3 seconds, more preferably 250 milliseconds to 2 seconds, most preferably 250 milliseconds to 1 second.

[0376] Aspect 36: The method according to any one of the preceding aspects, wherein the residence time of the particulate carbon-containing feedstock is 150 milliseconds to 4 seconds, preferably 200 milliseconds to 3 seconds, more preferably 250 milliseconds to 2 seconds, most preferably 250 milliseconds to 1 second, wherein the residence time is calculated according to equation (1);

[0377]

[0378] wherein t is the residence time, V is the reaction volume (in m3), Q is the volumetric flow (in m3*s-1). r is the residence time, V is the reaction volume (in m 3 3), Q is the volumetric flow (in m 3 3*s-1). -1 ​

[0379] Aspect 37. The method according to aspect 36, wherein the volumetric flow rate is the volume of fluid per second after injection of the particulate carbonaceous feedstock into the hot gas stream, preferably the fluid volume is calculated according to the ideal gas law according to equation (2):

[0380]

[0381] where Q is the volumetric flow rate of the fluid (in m3s 3 *s -1 ), is the sum of the molar flow rates of the gaseous species N2, CO2, CO, H2O, volatiles (in mol s -1 ), R is the gas constant, i.e. 8.3145 J K -1 · mol -1 , T is the absolute temperature, and P is the pressure.

[0382] Aspect 38. The method according to any one of aspects 35 to 37, wherein the residence time is chosen in such a way that the C, H containing species in the particulate carbonaceous feedstock are fully pyrolyzed.

[0383] Aspect 39. The method according to any one of the preceding aspects, wherein the method further comprises (e) quenching the hot gas stream after injection according to step (d).

[0384] Aspect 40. The method according to any one of the preceding aspects, wherein the hot gas stream is quenched (e) when the transmittance of the obtained carbon black at 425 nm is at least 20%, preferably at least 30%, more preferably at least 40%, still more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 relative to toluene.

[0385] Aspect 41. The method according to any one of the preceding aspects, wherein the transmittance of the produced carbon black at 425 nm is measured and the quenching position is adjusted until the transmittance of the produced carbon black at 425 nm is at least 20%, preferably at least 30%, more preferably at least 40%, still more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 relative to toluene.

[0386] The 42th aspect: The method according to any one of the preceding aspects, wherein the quenching position in the entrained-flow reactor is chosen in such a way that the transmittance of the produced carbon black at 425 nm is at least 20 %, preferably at least 30 %, more preferably at least 40 %, still more preferably at least 60 %, most preferably at least 80 %, wherein the transmittance at 425 nm is measured in toluene relative to toluene according to ASTM D 1618-18.

[0387] The 43th aspect: The method according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock is injected into the reactor with a mass flow of 2 kg / h to 50 kg / h per 130 L of the reaction volume of the reactor, preferably 5 kg / h to 40 kg / h per 130 L of the reaction volume of the reactor, more preferably 8 kg / h to 30 kg / h per 130 L of the reaction volume of the reactor, most preferably 10 kg / h to 20 kg / h per 130 L of the reaction volume of the reactor.

[0388] The 44th aspect: The method according to any one of the preceding aspects, wherein the reaction volume of the reactor is the volume of the reactor between the location where the particulate carbon-containing feedstock is injected and the quenching position.

[0389] The 45th aspect: The method according to any one of the 2th to 44th aspect, wherein the depolymerization is performed by (i) accelerating the particulate carbon-containing feedstock, and / or (ii) applying a shear force, preferably using an extruder.

[0390] The 46th aspect: The method according to any one of the 2th to 45th aspect, wherein the depolymerization is performed in (i) a feed mixing device, preferably a feed mixing device comprising a nozzle, and / or (ii) an extruder.

[0391] The 47th aspect: The method according to any one of the 2th to 46th aspect, wherein the depolymerization is performed in (i) a feed mixing device comprising a Laval nozzle.

[0392] The 48th aspect: The method according to any one of the 2th to 47th aspect, wherein the depolymerization is performed by placing the particulate carbon-containing feedstock in a carrier gas jet.

[0393] The 49th aspect: The method according to any one of the 2th to 48th aspect, wherein the depolymerization is performed in a feed mixing device for feeding particulate to the reactor, the feed mixing device comprising:

[0394] (i) a carrier gas channel extending through the feed mixing device,

[0395] (ii) at least one carrier gas inlet in fluid connection with the carrier gas channel,

[0396] (iii) at least one particle inlet,

[0397] (iv) a mixing chamber in fluid connection with the at least one particle inlet and the carrier gas inlet;

[0398] (v) a de-agglomeration conduit in fluid connection with the mixing chamber;

[0399] (vi) at least one outlet for the carrier gas entraining particles that have been fed to the mixing chamber, wherein the at least one outlet is in fluid connection with the de-agglomeration conduit; and

[0400] (vii) means for accelerating the carrier gas stream and injecting the carrier gas stream into the mixing chamber.

[0401] Aspect 50: The process according to any one of aspects 2 to 49, wherein the de-agglomerated particulate carbon-containing feedstock 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 bar to 1.3 bar, most preferably 0.8 bar to 1.2 bar.

[0402] Aspect 51 : The process according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock is comprised in a carrier gas.

[0403] Aspect 52: The process according to any one of aspects 2 to 51, wherein the de-agglomerated particulate carbon-containing feedstock is comprised in a carrier gas.

[0404] Aspect 53: The process according to any one of aspects 2 to 52, wherein the de-agglomerated particulate carbon-containing feedstock is comprised in a carrier gas, and the carrier gas further comprises H2O and / or an additive.

[0405] Aspect 54: The process according to any one of aspects 2 to 53, wherein the de-agglomerated particulate carbon-containing feedstock is comprised in a carrier gas, and the carrier gas further comprises 1 vol.% to 10 vol.% H2O, based on the total volume of the carrier gas comprising the de-agglomerated particulate carbon-containing feedstock.

[0406] Aspect 55: The process according to any one of the preceding aspects, wherein the particulate carbon-containing feedstock is injected into the entrained-flow reactor through a plurality of inlets, preferably through a plurality of lances.

[0407] Aspect 56: The process according to any of the preceding aspects, wherein the particulate carbon-containing feedstock is fractionated, preferably sieved, prior to injecting the particulate carbon-containing feedstock into the reactor, preferably (a) the sieve has a mesh size of 2000 pm, 1000 pm, 500 pm, 250 pm or 125 pm, preferably 500 pm, 250 pm or 125 pm, and / or (b) the sieve has a pore size that retains particles having a size of greater than 2000 pm, greater than 1000 pm, greater than 500 pm, greater than 250 pm or greater than 125 pm, preferably greater than 500 pm, greater than 250 pm or greater than 125 pm.

[0408] Aspect 57: The process according to any of the preceding aspects, wherein at least 70 wt.%, preferably at least 80 wt.%, more preferably at least 90 wt.%, most preferably at least 98 wt.% of the particulate carbon-containing feedstock has a particle size of less than 2 mm, preferably less than 1 mm, more preferably less than 500 pm, most preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0409] Aspect 58: The process according to any of the preceding aspects, wherein at least 70 wt.%, preferably at least 80 wt.%, more preferably at least 90 wt.%, most preferably at least 98 wt.% of the particulate carbon-containing feedstock has a particle size of less than 500 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0410] Aspect 59: The process according to any of the preceding aspects, wherein at least 70 wt.%, preferably at least 80 wt.%, more preferably at least 90 wt.%, most preferably at least 98 wt.% of the particulate carbon-containing feedstock has a particle size of less than 1 mm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0411] Aspect 60: The process according to any of the preceding aspects, wherein at least 70 wt.%, preferably at least 80 wt.%, more preferably at least 90 wt.%, most preferably at least 98 wt.% of the particulate carbon-containing feedstock has a particle size of less than 2 mm, preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0412] Aspect 61 : Carbon black produced according to the process of any of the preceding aspects, and / or

[0413] (I) carbon black having a BET surface area of 80 m 2 / g to 90 m 2 / g, with a compressive oil absorption value of 58mL / 100g to 69mL / 100g, wherein the BET surface area was measured according to ASTM D6556-21, and the compressive oil absorption value was measured using paraffin oil according to ASTM D3493-20;

[0414] and / or

[0415] (II) Carbon black with the following properties: BET surface area of ​​70m² 2 / g to 85m 2 / g, with a compression oil absorption value of 59mL / 100g to 70mL / 100g, wherein the BET surface area is measured according to ASTM D6556-21, and the compression oil absorption value is measured using paraffin oil according to ASTM D3493-20;

[0416] and / or

[0417] (III) Carbon black with the following properties: BET surface area of ​​80m² 2 / g to 96m 2 / g, with a compression oil absorption value of 60mL / 100g to 69mL / 100g, wherein the BET surface area is measured according to ASTM D6556-21, and the compression oil absorption value is measured using paraffin oil according to ASTM D3493-20;

[0418] and / or

[0419] (IV) Carbon black with the following properties: BET surface area of ​​120 m² 2 / g to 138m 2 / g, with a compressive oil absorption value of 58mL / 100g to 69mL / 100g, wherein the BET surface area was measured according to ASTM D6556-21, and the compressive oil absorption value was measured using paraffin oil according to ASTM D3493-20;

[0420] and / or

[0421] (V) Carbon black with the following properties: BET surface area of ​​82m² 2 / g to 95m 2 / g, with a compressive oil absorption value of 59mL / 100g to 70mL / 100g, wherein the BET surface area is measured according to ASTM D6556-21, and the compressive oil absorption value is measured using paraffin oil according to ASTM D3493-20.

[0422] Aspect 61b: According to the carbon black of aspect 61, wherein...

[0423] (I) Carbon black (I) preferably has a BET surface area of ​​85m² 2 / g to 88m 2 / g, preferably a Compressed Oil Uptake of 61 mL / 100 g to 64 mL / 100 g, preferably an STSA surface area of 72 m 2 / g to 82 m 2 / g, more preferably an STSA surface area of 76 m 2 / g to 79 m 2 / g, preferably a Compressed Oil Uptake of 61 mL / 100 g to 64 mL / 100 g, preferably an STSA surface area of 72 m

[0424] (II) Carbon Black (II) preferably a BET surface area of 77 m 2 / g to 79 m 2 / g, preferably a Compressed Oil Uptake of 61 mL / 100 g to 64 mL / 100 g, preferably an STSA surface area of 72 m 2 / g to 78 m 2 / g, more preferably an STSA surface area of 71 m 2 / g to 73 m 2 / g, preferably a Compressed Oil Uptake of 61 mL / 100 g to 64 mL / 100 g, preferably an STSA surface area of 72 m

[0425] (III) Carbon Black (III) preferably a BET surface area of 89 m 2 / g to 92 m 2 / g, preferably a Compressed Oil Uptake of 61 mL / 100 g to 64 mL / 100 g, preferably an STSA surface area of 72 m 2 / g to 87 m2 / g, more preferably STSA surface area of 82 m 2 / g to 84 m 2 / g, preferably volatiles of 2.2 wt% to 2.9 wt%, more preferably volatiles of 2.5 wt% to 2.7 wt%, preferably transmittance in toluene at 425 nm greater than 40%, more preferably transmittance in toluene at 425 nm greater than 62%, wherein BET surface area is measured according to ASTM D6556-21, compressive oil absorption is measured according to ASTM D3493-20 using paraffinic oil, STSA surface area is measured according to ASTM D6556-21, volatiles are measured according to described in the specification at 950 °C for 7 minutes, and transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene; and / or

[0426] (IV) Carbon black (IV) preferably BET surface area of 127 m 2 / g to 130 m 2 / g, preferably compressive oil absorption of 62 mL / 100g to 64 mL / 100g, preferably STSA surface area of 82 m 2 / g to 95 m 2 / g, more preferably STSA surface area of 87 m 2 / g to 89 m 2 / g, preferably volatiles of 2.6 wt% to 3.2 wt%, more preferably volatiles of 2.8 wt% to 3.0 wt%, preferably transmittance in toluene at 425 nm greater than 60%, more preferably transmittance in toluene at 425 nm greater than 80%, wherein BET surface area is measured according to ASTM D6556-21, compressive oil absorption is measured according to ASTM D3493-20 using paraffinic oil, STSA surface area is measured according to ASTM D6556-21, volatiles are measured according to described in the specification at 950 °C for 7 minutes, and transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene; and / or

[0427] (V) Carbon black (V) preferably BET surface area of 86 m 2 / g to 89 m 2 / g, preferably compressive oil absorption of 63 mL / 100g to 65 mL / 100g, preferably STSA surface area of 70 m 2 / g to 82 m 2 / g, more preferably STSA surface area of 76 m 2 / g to 78 m 2 / g, preferably the volatile matter is 1.8 wt.-% to 2.4 wt.-%, more preferably the volatile matter is 2.0 wt.-% to 2.2 wt.-%, preferably the transmittance at 425 nm in toluene is more than 60 %, more preferably the transmittance at 425 nm in toluene is more than 80 %, wherein the BET surface area is measured according to ASTM D6556-21, the compressive oil absorption is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatile matter is measured according to the description at 950 °C for 7 min and the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 relative to toluene.

[0428] Aspect 62: A composition comprising

[0429] (A) an elastomeric polymeric material, and

[0430] (B) the carbon black obtained according to any one of aspects 1 to 61 and 61b.

[0431] Aspect 63: An article made from or comprising the composition according to aspect 62.

[0432] Aspect 64: Use of a particulate carbon-containing feedstock for the manufacture of carbon black in an entrained-flow reactor.

[0433] Aspect 65: The use according to aspect 64, wherein at least 70 wt.-%, preferably at least 80 wt.-%, more preferably at least 90 wt.-%, most preferably at least 98 wt.-% of the particulate carbon-containing feedstock have a particle size of less than 2 mm, preferably less than 1 mm, more preferably less than 500 pm, most preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511 -12 (2017).

[0434] Aspect 66: The use according to any one of aspects 64 and 65, wherein the particulate carbon-containing feedstock has a residence time of 150 milliseconds to 4 seconds, preferably 200 milliseconds to 3 seconds, more preferably 250 milliseconds to 2 seconds, most preferably 250 milliseconds to 1 second, wherein the residence time is calculated according to equation (1);

[0435]

[0436] wherein t r is the residence time, V is the reaction volume in m 3 , Q is the volume flow in m 3 * s -1 .

[0437] 67. The use according to any one of aspects 64 to 66, wherein a depolymerized particulate carbonaceous raw material is used.

[0438] Aspect 68: A method for adjusting the quench position in an entrained fluidized bed reactor for producing carbon black from particulate carbonaceous feedstock, the method comprising:

[0439] I) Injecting granular carbonaceous raw material into a hot gas stream in an entrained fluidized bed reactor, wherein the temperature of the hot gas stream is at least 800°C.

[0440] Ⅱ) Rapidly cool the hot gas stream containing the produced carbon black.

[0441] Ⅱ) Measure the transmittance of the produced carbon black.

[0442] III) Adjust the quench position in the fluidized bed reactor until the transmittance of the produced carbon black is at least 20%, preferably at least 30%, more preferably at least 40%, even more preferably at least 60%, and most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured relative to toluene according to ASTM D1618-18.

[0443] Example

[0444] Example 1 : Rubber particles

[0445] like Figure 1 As shown, the experiment of Example 1 was carried out on a small furnace reactor. The furnace reactor includes a combustion chamber, a throat section, and a channel. The throat section has a diameter reduced to 45 mm. A reactor channel with a diameter of 200 mm and a length of 4200 mm was installed downstream of the throat section.

[0446] like Figure 2 As shown, rubber granules are injected into the throat section of a furnace reactor through a feed mixing device equipped with nozzles. The reaction volume of the reactor is approximately 130 L. The reaction volume refers to the reactor volume between the feed injection point and the quenching point. The feed mixing device accelerates the deagglomeration of the rubber granules by accelerating the production of granular carbonaceous feedstock. However, the invention is not limited to the present invention. Figure 1 The feed mixing device is not specified, therefore other feed mixing devices can be used. The rubber granules used in the experiment, namely 0.0 to 0.5 mm Gummigranulat (trade number 005GUM), were supplied by ESTATO Umweltservice GmbH (ESTATO), Germany. The rubber granules were derived from used tires, including synthetic rubber (SBR) and natural rubber (NR). The particle size is shown in Table 1. In addition, the weight-average particle size (Dw50) measured according to ASTM D 1511-12 (2017) is approximately 400 μm. However, different granular carbonaceous raw materials, such as plastic granules or biomass-based granules, can also be used.

[0447] Table 1 : Particle distribution of rubber particles from ESTATO company measured according to ASTM D 1511-12 (2017).

[0448]

[0449]

[0450] The properties of the rubber particles from ESTATO company are shown in Table 2.

[0451] Table 2: Properties of rubber particles from ESTATO company.

[0452] Performance Measurement Unit Value Carbon mass fraction Refer to the following method ％ 87.623 Hydrogen mass fraction Refer to the following method ％ 7.767 Nitrogen mass fraction Refer to the following method ％ 0.396 Sulfur mass fraction Refer to the following method ％ 2.022 Oxygen mass fraction Refer to the following method ％ 2.191 Water content ASTM D 4928-12 (2018) ％ 2.19 Ash content ASTM D 1506-99, 550 °C, 16 hours ％ 11.29 Total heat value ASTM D 4809:2018 MJ / kg 35.121

[0453] In addition, the rubber particles contain several metals in a mass fraction of about 300 ppm. For example, zinc and iron.

[0454] CHNS content determined with elemental analyzer

[0455] The carbon mass fraction, hydrogen mass fraction, nitrogen mass fraction and sulfur mass fraction were measured using an elemental analyzer with a thermal conductivity and infrared detector. The elemental analyzer is a device for the fully automated quantitative analysis of the above-mentioned elements. The combustion tube is heated to 1100 °C and the reduction tube to 850 °C. First, a blank measurement is carried out. The value of the carbon peak area should be less than 50, the value of the hydrogen peak area should be less than 300, the value of the nitrogen peak area should be less than 50 and the value of the sulfur peak area should be less than 350. Otherwise, the individual adsorption columns are heated and the blank measurement is then started again. The blank measurement value is calculated as follows:

[0456]

[0457] where b is the blank measurement value, b i 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.

[0458] The compensation of the blank measurement value is calculated as follows:

[0459] acomp. = a - b

[0460] where acomp. is the area of the compensated peak, a is the measured peak area and b is the blank measurement value.

[0461] Next, the daily factor is measured. For this, 3 mg of sulfanilamide and 3 mg of a low-level standard (e.g. carbon black standard) are weighed into 8 tin capsules. After weighing the respective samples, they are placed into the capsule press, overlaid with helium for 35 seconds and then cold-sealed. Subtracting the blank value, the known theoretical element concentration of the standard sample is compared to the actually calculated element concentration. From this, the daily factor is derived, which must be between 0.9 and 1.1. If this is not the case, the measurements should be repeated using a freshly opened standard. Otherwise, a new calibration must be carried out according to the manufacturer's instructions.

[0462] The daily factor is calculated as follows:

[0463]

[0464] where f is the daily factor, c 理论 is the theoretical factor, c 实际 is the actually calculated element concentration.

[0465] Then, 8 tin capsules are weighed, each containing 5 mg ± 1 mg of the desired measurement component, e.g. rubber particles. After weighing the individual samples, they are placed into the capsule press, covered with helium for 35 seconds and then cold-welded.

[0466] For the measurement, the combustion tube is enriched with oxygen. The elements C, H, N and S are combusted to form CO2, H2O, NOx, SO2 and SO3. The bound halogens in the sample react to form volatile halogen compounds. In addition, there are WO3 particles in the combustion tube, which provide more O2 as catalyst, prevent the formation of non-volatile sulfate salts and bind interfering alkaline and alkaline earth elements. The carrier gas stream is fed into a reduction tube filled with copper. The nitrogen oxides (NOx) are completely reduced to N2 at the copper contact. SO3 is reduced to SO2. The volatile halogen compounds are bound to silver wires.

[0467] N2 is not adsorbed and enters the thermal conductivity detector as the first measurement component, CO2, H2O and SO2 are adsorbed on the respective adsorption columns.

[0468] Then, one after the other, the adsorption columns are brought to the desorption temperature, so that CO2, then H2O as carrier gas enter the thermal conductivity detector and SO2 enters the infrared detector. Depending on the type and concentration of the components, the detector outputs electrical signals that are digitized and integrated. The measurement signals are recorded as a function of time and displayed as integral values. From the integral values of the individual measurement peaks and the calibration factor, the absolute element content of the sample is calculated.

[0469] The element concentration is calculated according to the following equation:

[0470]

[0471] where c is the element concentration in % units, a is the absolute element content in mg units, f is the daily factor and w is the actual sample weight.

[0472] O content determined with elemental analyzer

[0473] The electrical signal is transferred from the thermal conductivity detector (WLD) of the elemental analyzer to the microcontroller according to the oxygen concentration and then displayed as an integral value. From the integral value of the measured peak and the calibration factor, the absolute element content of the sample is derived.

[0474] The pyrolysis tube is heated to 1050 °C. First, a blank measurement is performed. The maximum of the oxygen peak area should be 200. If the blank value is not lower than 200, the CO adsorption column should be heated (260 °C, CO desorption 150 °C). After a successful blank measurement, the average of the blank value area is calculated.

[0475] The blank measurement value is calculated as follows:

[0476]

[0477] where b is the blank measurement value, b i is the peak area of the corresponding blank measurement, n is the number of blank measurements and i is an index from 1 to n.

[0478] Next, the daily factor is measured. For this, 3 mg sulfanilamide are weighed into 8 tin capsules. After weighing the corresponding samples, they are put into the capsule press, overlaid with helium for 35 seconds and then cold-sealed. Subtracting the blank value, the known theoretical element concentration of the standard sample is compared to the actually calculated element concentration. From this, the daily factor is derived, which must be between 0.9 and 1.1. If this is not the case, these measurements should be repeated using a newly opened standard. Otherwise, a new calibration must be performed according to the manufacturer’s instructions.

[0479] The daily factor is calculated as follows,

[0480]

[0481] where f is the daily factor, c 理论 is the theoretical factor and c 实际 is the actually calculated element concentration.

[0482] Then, 8 tin capsules are weighed, each containing 5 mg ± 1 mg of the desired measurement component, for example rubber particles. After weighing the individual samples, they are put into the capsule press, covered with helium for 35 seconds and then cold-welded. The samples are then measured.

[0483] The element concentration is calculated according to the following equation:

[0484]

[0485] where c is the element concentration in % units, a is the absolute element content in mg units, f is the daily factor, and w is the actual sample amount.

[0486] Reaction conditions in the furnace reactor

[0487] The reaction conditions for the preparation of carbon black are shown in Table 3. The temperature of the hot gas stream after injection of the feedstock was calculated as described in the description. The temperature (in absolute temperature) can also be measured with a pyrometer as described above. In addition, the residence time of particles with a diameter of 0.5 mm and 1 mm was calculated. The calculations were performed using a pyrolysis modeling program.

[0488] Table 3: Reaction conditions in the furnace reactor.

[0489]

[0490]

[0491] 1 273.15 K and 101325 Pa

[0492] 2 The k value is defined by the ratio of the amount of stoichiometric O2 required for complete stoichiometric combustion of the fuel to the amount of O2 supplied

[0493] Table 2: continuation

[0494] Experiment A6 A7 A8 A9 A10 combustion air stream (STP) 1 / m 3 / h]]> 150 150 150 150 150 Natural gas stream (STP) / m 3 / h]] 13.9 12.43 10.8 12.4 12.4 K value 2 ]] 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 rate (STP) / m 3 / h]] 5.7 7.1 6.5 6.7 7.5 Rubber particle mass flow / kg / h 11 18 16 18 18 O2 mole fraction at the charge point of the reactor / % 7.3 5 4.9 5 3.9 Calculated hot gas temperature / °C 1763 1640 1592 1645 1632 Residence time / s 0.367 0.383 0.391 0.383 0.383 Optimum residence time for particles with a diameter of 0.5 mm at the calculated temperature / s 0.28 0.315 0.32 0.31 0.32 Optimum residence time for particles with a diameter of 1 mm at the calculated temperature / s 1.05 1.11 1.22 1.125 1.125

[0495] After injection of the rubber particulate feedstock, the reaction was quenched with water, the obtained carbon black was dried and ground to obtain a volume average particle size of about 5 pm. The carbon black obtained according to the application (see experiments A1 to E12) was compared with standard carbon black N660 and recycled carbon black rCB. rCB was recycled from the pyrolysis of rubber particles.

[0496] The temperature in the combustion chamber, i.e. the temperature of the hot combustion gases, was controlled by the combustion air temperature 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) into the combustion chamber.

[0497] The produced carbon black comprises about 53 wt% recycled carbon black, about 27 wt% new carbon black and about 20 wt% ash. The recycled carbon black comprises coke. Due to the use of rubber particles for the entrained flow reactor process, not only carbon black can be recycled, but also new carbon black originating from the rubber can be produced. Therefore, the ash content is lower compared to the carbon black recycled from REOIL (RCB615, about 23.2 wt% ash). The ash content can be measured according to ASTM D 1506-99 at 550 °C for 16 hours.

[0498] The carbon blacks obtained in each experiment were characterized, the results are shown in Table 4.

[0499] Table 4: Properties of the obtained carbon blacks

[0500] Experiment B1 B2 B3 B4 B5 B6 B7 Carbon black [N550 3 ]]> [N660 4 ]]> rCb 5 ]]> A1 A2 A3 A4 Agglomerate size 6 , number average / nm 212 208 98 n / a n / a 46 46 Agglomerate size 6 , weight average / nm 167 n / a n / a 102 106 Agglomerate size 6 , weight mode / nm 172 156 n / a n / a 70 74 Specific surface area 7 (AGV) / m 2 / g]]> 24 n / a n / a 42.6 41.3 Volatile matter 8 / weight percent 4.5 n / a n / a 2.4 2.3 BET surface area 9 / m 2 / g]]> 39 35.1 72.4 n / a 117.4 86.6 78.2 STSA surface area 10 / m 2 / g]]> 38.75 34.55 60.9 n / a 91 77.8 72.1 Iodine adsorption value 11 ]]> 42.7 36.6 94.5 n / a n / a 101.1 77.8 pH 12 ]] 8.7 8.4 7.32 n / a n / a 7.42 7.38 Compressed oil absorption number (COAN) 13 / ml / 100 g 83.9 72 80.2 n / a n / a 62.2 64.4 Oil absorption number (OAN) 14 ]] 120.95 90.35 92.3 n / a n / a 64 68.6 Transmittance 15 / %]] 97 92.7 n / a n / a 94.9 78.7 57.5

[0501] 3 N550, from Orion Engineered Carbon GmbH, liquid feedstock

[0502] Carbon black obtained from liquid feedstock

[0503] 4 N660, from Orion Engineered Carbon GmbH, liquid feedstock

[0504] Carbon black obtained from liquid feedstock

[0505] 5 rCB 2, recycled carbon black, REOIL S.P.ZO.O

[0506] 6 The agglomerate size distribution was measured as described below.

[0507] 7 The specific surface area (AGV) was measured as described below.

[0508] 8 The volatiles were measured at 950 °C for 7 minutes as described below

[0509] 9 The BET surface area was measured according to ASTM D6556-21.

[0510] 10 The STSA surface area was measured according to ASTM D6556-21.

[0511] 11 The iodine adsorption value was measured according to ASTM D 1510-21.

[0512] 12 pH value was measured according to ASTM D 1512-21, Test Method B - Sonic Pulp

[0513] 13 Compressed oil absorption number (COAN) was measured according to ASTM D3493-20 (using paraffinic oil)

[0514] 14 Oil absorption number (OAN) was measured according to ASTM D 2414-19 (using paraffinic oil)

[0515] 15 Transmittance in toluene at 425 nm (transmittance of toluene extract) was measured according to ASTM D 1618-18 versus toluene.

[0516] Table 4: Continued

[0517] Experiment B8 B9 B10 B11 B12 B13 Carbon black A5 A6 A7 A8 A9 A10 Agglomerate size 6 , number average / nm 42 41 47 49 n / a n / a Agglomerate size 6 , weight average / nm 105 102 108 105 n / a n / a Agglomerate size 6 , weight mode / nm 74 73 76 72 n / a n / a Specific surface area 7 (AGV) / m 2 / g]]> 42 43.9 40.2 40.6 n / a n / a Volatile matter 8 / weight percent 2.6 2.9 2.2 2.1 n / a n / a BET surface area 9 / m 2 / g]]> 90.9 128.6 n / a 87.5 84.2 79.5 STSA surface area 10 / m 2 / g]]> 83.2 88.4 n / a 77.1 77 75.1 Iodine adsorption value 11 ]]> 94.4 129.2 93.2 99.7 n / a n / a pH 12 ]]> 7.36 7.06 7.23 8.01 n / a n / a Compressed oil absorption number (COAN) 13 / ml / 100 g 64.5 63.4 63.7 64.3 n / a n / a Oil absorption number (OAN) 14 ]]> 68 66.5 70.6 67.2 n / a n / a Transmittance 15 / %]] 63 95 52.8 86 66.9 48.6

[0518] Agglomerate size distribution

[0519] All test results were analyzed using a Brookhaven BI-DCP disc centrifuge with a red light diode according to ISO 15825:2016. The test results were provided in the Brookhaven software after appropriate parameter adjustments described in ISO 185825:2017-03 section “Computer and Software Setup”.

[0520] Specific surface area (AGV

[0521] The specific surface area of the test sample was available in the Brookhaven software. After the sample test and review of the results, click on the “Details” results to read the “Specific Surface Area sq / g” value on the computer display.

[0522] Volatiles at 950 °C

[0523] ​The volatile matter at 950 °C was measured according to the following protocol using a thermogravimetric analyzer (TGA-701) from Fa. LECO Instrumente GmbH: The sample pan was dried at 650 °C for 30 minutes. Prior to the measurement, the carbon black material was stored in a desiccator with a drying agent. The oven-dried sample pan was loaded into the instrument, weighed and filled with 0.5 g to 10 g of the carbon black material. Then, the oven of the TGA instrument with the sample pan was heated up to 105 °C by automatic software control and the sample was dried until a constant mass was reached. Subsequently, the sample pan was covered with a lid, the oven was purged with nitrogen (99.9 vol.-% grade) and heated to 950 °C. The oven temperature was held at 950 °C for 7 minutes. The content of volatile matter at 950 °C was calculated using the following equation:

[0524]

[0525] Results

[0526] Surprisingly, it was found that a particulate carbonaceous feedstock can be used in an entrained flow reactor process. As can be seen from Table 3, the obtained carbon black has desirable properties compared to standard carbon black products obtained from liquid carbonaceous feedstocks.

[0527] Furthermore, the agglomerate size as well as the agglomerate surface area is low compared to the agglomerate size and the agglomerate surface area of the recycled carbon black. This indicates that the obtained carbon black has a low coke content. The specific surface area measurement of the agglomerate size further indicates the amount of coke present in the carbon black. Furthermore, a large agglomerate size also indicates a high coke content.

[0528] Furthermore, as can be seen from Table 3, the residence time of A6 is 0.367 seconds and the temperature of the hot gas stream is 1763 °C. It is generally accepted that a higher temperature leads to an optimal residence time of 0.28 seconds for a particle having a diameter of 0.5 mm and an optimal residence time of 1.05 seconds for a particle having a diameter of 1 mm. The transmittance in experiment B9 using A6 is 95 %. The transmittance is an indicator for the complete pyrolysis of the feedstock or the C, H containing compounds in the feedstock. Therefore, it is generally accepted that a higher temperature and a longer residence time are beneficial for the production of carbon black from a particulate feedstock.

[0529] Example 2: Rubber composition

[0530] The preparation of the rubber compositions and the rubber tests are described below. The general methods for producing rubber compounds and vulcanizates thereof are described in the book “Rubber Technology Handbook”, W. Hofmann, Hanser Verlag 1994.

[0531] The rubber compositions are listed in Table 5. ESBR Buna SB 1500 was introduced into a laboratory mixer GK1.5E with intermeshing PES5 rotor geometry manufactured by Harburg Freudenberger and milled for 30 seconds at a room temperature of 40 °C, a fill factor of 0.66 and a rotor speed of 45 revolutions per minute. Subsequently, half the volume of carbon black, ZnO and stearic acid was added during milling. After 90 seconds, the other half of the volume of carbon black and 6PPD was added. After a further 90 seconds, the ram was lifted and cleaned and the batch was then mixed for a further 90 seconds. The total mixing time in the internal mixer was 5 minutes, after which the batch was poured onto an open mill for cooling and additional distribution mixing. The batch temperature did not exceed 160 °C in the first mixing step. The batch was allowed to rest overnight.

[0532] In the second and final mixing step, the sulfur and accelerant (Vulkacit CZ / EG-Z) were added to the master batch obtained from the first mixing step in the specified amounts. The resulting mixture was milled in a GK1.5E mixer for 2 minutes at a chamber temperature of 40 °C and a fill factor of 0.64. The rotor speed was 30 revolutions per minute, ensuring that the batch temperature did not exceed 110 °C. Finally, the mixture was poured from the internal mixer and processed again on an open mill. The resulting vulcanizable composition (green compound) was cured for 11 minutes to 15 minutes at a temperature of 165 °C (C1 : 15 minutes, C2: 12 minutes, C3: 12 minutes, C4: 12 minutes; C5: 11 minutes, C6: 12 minutes, C7: 12 minutes, C8: 11 minutes, C9: 11 minutes).

[0533] Table 5: Rubber compositions using different carbon blacks as shown in Table 6.

[0534] 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

[0535] 16 Rubber ESBR, Buna SB 1500, Resinex Deutschland GmbH

[0536] 17 Carbon black: N660, N550, rCB or experiments A3 to A5 and A8 to A10 (see Table 6)

[0537] 18 6PPD, VULKANOX 4020 / LG, Brenntag GmbH

[0538] 19 Sulfur, ground sulfur (MAHLSCHWEFEL) 80 / 90° oil-free, Avokal GmbH

[0539] 20 CBS, VULKACIT CZ / EG-C, Lanxess N.V.

[0540] 21 ZnO, ZNO RS RAL 844C, Norkem B.V.

[0541] 22 Stearic acid, Palmera B 1804, Caldic Deutschland GmbH

[0542] The properties of the test specimens were measured and the results are shown in Table 6. The results are compared with carbon blacks produced using liquid carbon black feedstocks (N660 and N550) and recycled carbon black rCB.

[0543] Table 6: Properties of carbon blacks produced in rubber compositions.

[0544]

[0545] 23 The loss factor tan(d) was measured as described below.

[0546] 24 The morphology relative peak area was measured as described below.

[0547] 25 The tensile strength was measured according to ISO 37-2012 S2.

[0548] 26 The elongation at break was measured according to ISO 37-2012 S2.

[0549] 27 The abrasion was measured according to DIN ISO 4649:2014-03 at 23 °C at 10 N.

[0550] 28 The modulus 300% was measured according to ISO 37-2012 S2.

[0551] 29 The ball rebound was measured according to ASTM D 2632:2015 at 60 °C.

[0552] 30 The GRAVES tear resistance was measured according to DIN ISO 34-1 :2016-09 Method B deformation type (b).

[0553]

[0554] Morphology relative peak area

[0555] The topography relative peak area is an indicator of filler dispersibility including the Medalia correction by surface topography according to the procedure described in A. Wehmeier, "Filler Dispersion Analysis by Topography Measurements", Technical Report TR 820, Degussa GmbH and A. Wehmeier, "Entwicklung eines Verfahrens zur Charakterisierung der Füllstoffdispersion in Gummimischungen mittels einer Oberflachentopographie", Thesis, 1998 at the Münster University of Applied Sciences, and DE 199 17 975 C2.

[0556] Loss factor tan(d)

[0557] The above values and the loss factor tan(d) are measured according to DIN 53513 at 60 °C with a frequency of 16 Hz in strain controlled mode (1 ± 0.5 mm) or force controlled mode (50 N ± 25 N) on cylindrical test specimens (10 mm high, 10 mm in diameter) tan (d).

[0558] Results

[0559] The examples show that the carbon blacks produced according to the application (carbon blacks A3 to A5, A8 to A10) can be used advantageously in rubber compositions (experiments C5 to C10). The carbon blacks produced have a low loss factor tan(d) while at the same time having a high topography value and a high tensile strength. In addition, the elongation at break is advantageously between 612% and 665%. The ball rebound of the carbon blacks produced is comparable to the ball rebound of carbon black N660 and carbon black N550.

[0560] It is to be understood that various modifications can be made, and many changes can be made in the preferred embodiments without departing from the principles of the present application.

Claims

1. A process for producing carbon black from a particulate carbon-containing feedstock in an entrained-flow reactor having a flow channel along a longitudinal axis of the reactor center, the process comprising: (a) providing a hot gas stream, (b) providing a particulate carbon-containing feedstock, and (d) injecting the particulate carbon-containing feedstock into the hot gas stream to form carbon black, wherein the hot gas stream has a temperature of at least 800 °C.

2. The process according to claim 2, wherein the particulate carbon-containing feedstock comprises rubber particles, plastic particles and / or biomass-based particles, preferably the particulate carbon-containing feedstock comprises rubber particles, wherein the rubber particles comprise carbon black.

3. The process according to any one of claim 1 or claim 2, wherein at least 70 wt.-%, preferably at least 80 wt.-%, more preferably at least 90 wt.-%, most preferably at least 98 wt.-% of the particulate carbon-containing feedstock have a particle size of less than 2 mm, preferably less than 1 mm, more preferably less than 500 pm, most preferably less than 250 pm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

4. The process according to any one of the preceding claims, wherein the particle size distribution of the particulate carbon-containing feedstock is measured according to ASTM D 1511-12 (2017) and: (a) 1 wt.-% to 0 to 10 wt.-%, preferably 1 wt.-% to 8 wt.-%, more preferably 1 wt.-% to 5 wt.-%, most preferably 1 wt.-% to 3 wt.-% of the particulate carbon-containing feedstock is retained by the No. 10 sieve, and / or (b) 1 wt.-% to 25 wt.-%, preferably 2 wt.-% to 20 wt.-%, more preferably 4 wt.-% to 15 wt.-%, most preferably 5 wt.-% to 12 wt.-% of the particulate carbon-containing feedstock is retained by the No. 18 sieve, and / or (c) 10 wt.-% to 80 wt.-%, preferably 15 wt.-% to 70 wt.-%, more preferably 20 wt.-% to 60 wt.-%, most preferably 25 wt.-% to 55 wt.-% of the particulate carbon-containing feedstock is retained by the No. 35 sieve, and / or (d) 5 wt.-% to 70 wt.-%, preferably 10 wt.-% to 60 wt.-%, more preferably 15 wt.-% to 50 wt.-%, most preferably 20 wt.-% to 45 wt.-% of the particulate carbon-containing feedstock is retained by the No. 60 sieve, and / or (e) 1 wt.-% to 80 wt.-%, preferably 7 wt.-% to 70 wt.-%, more preferably 5 wt.-% to 60 wt.-%, most preferably 7 wt.-% to 50 wt.-% of the particulate carbon-containing feedstock is retained by the No. 120 sieve, and / or (f) the bottom receiving pan contains less than 4 wt.-%, preferably less than 3 wt.-%, more preferably 0 to 2 wt.-%, most preferably 0.01 wt.-% to 1 wt.-% of the particulate carbon-containing feedstock.

5. The process according to any one of the preceding claims, wherein the hot gas stream is obtained by electric preheating, plasma heating and combustion of a fuel and an oxygen-containing gas, and / or wherein the entrained-flow reactor is a furnace reactor.

6. The process according to any one of the preceding claims, wherein the particulate carbon- containing feedstock is fractionated, preferably sieved, prior to injection into the reactor, preferably (a) the sieve has a mesh size of 2000 pm, 1000 pm, 500 pm, 250 pm or 125 pm, preferably 500 pm, 250 pm or 125 pm, and / or (b) the sieve has a pore size that retains particles having a size of greater than 2000 pm, greater than 1000 pm, greater than 500 pm, greater than 250 pm or greater than 125 pm, preferably greater than 500 pm, greater than 250 pm or greater than 125 pm.

7. The process according to any one of the preceding claims, wherein the residence time of the particulate carbon-containing feedstock is from 150 milliseconds to 4 seconds, preferably from 200 milliseconds to 3 seconds, more preferably from 250 milliseconds to 2 seconds, most preferably from 250 milliseconds to 1 second, wherein the residence time is calculated according to equation (1); where t r is the residence time, V is the reaction volume (in m 3 ), and Q is the volumetric flow (in m 3 *s -1 ).

8. The process according to any one of the preceding claims, wherein the quench location in the entrained-flow reactor is selected in such a way that the transmittance of the produced carbon black at 425 nm is at least 20%, preferably at least 30%, more preferably at least 40%, still more preferably at least 60%, most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured according to ASTM D 1618-18 against toluene.

9. The process according to any one of the preceding claims, wherein the particulate carbon- containing feedstock is injected into the reactor with a mass flow of from 2 kg / h to 50 kg / h per 130 L of reaction volume of the reactor, preferably from 5 kg / h to 40 kg / h per 130 L of reaction volume of the reactor, more preferably from 8 kg / h to 30 kg / h per 130 L of reaction volume of the reactor, most preferably from 10 kg / h to 20 kg / h per 130 L of reaction volume of the reactor.

10. The process according to any one of the preceding claims, wherein step (b) further comprises subjecting the particulate carbon-containing feedstock to depolymerization, and in step (d) the depolymerized particulate carbon-containing feedstock is injected into the hot gas stream to form carbon black, wherein the depolymerization is performed by (i) accelerating the particulate carbon-containing feedstock, and / or (ii) applying a shear force, preferably using an extruder.

11. Carbon black produced according to the process of any one of the preceding claims, and / or (I) carbon black having a BET surface area of 80 m 2 / g to 90 m 2 / g, preferably a BET surface area of 85 m 2 / g to 88 m 2 / g, and a compression oil absorption of from 58 mL / 100 g to 69 mL / 100 g, preferably a compression oil absorption of from 61 mL / 100 g to 64 mL / 100 g, Preferably the STSA surface area is 72 m 2 / g to 82 m 2 / g, more preferably the STSA surface area is 76 m 2 / g to 79 m 2 / g, preferably volatiles of from 2.1 wt% to 2.7 wt%, more preferably volatiles of from 2.3 wt% to 2.5 wt%, preferably a transmittance in toluene at 425 nm of greater than 50%, more preferably a transmittance in toluene at 425 nm of greater than 77%, wherein the BET surface area is measured according to ASTM D6556-21, the Compressed Oil Uptake is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to described in the specification at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene; and / or (II) carbon black having a BET surface area of 70 m 2 / g to 85 m 2 / g, preferably a BET surface area of 77 m 2 / g to 79 m 2 / g, and the Compressed Oil Uptake is 59 mL / 100g to 70 mL / 100g, preferably the Compressed Oil Uptake is 63 mL / 100g to 65 mL / 100g, Preferably the STSA surface area is 68 m 2 / g to 78 m 2 / g, more preferably the STSA surface area is 71 m 2 / g to 73 m 2 / g, preferably the Compressed Oil Uptake is 58 mL / 100g to 69 mL / 100g, more preferably the Compressed Oil Uptake is 63 mL / 100g to 65 mL / 100g, preferably the volatiles are 2.0 wt% to 2.6 wt%, more preferably the volatiles are 2.2 wt% to 2.4 wt%, preferably the transmittance in toluene at 425 nm is greater than 40%, more preferably the transmittance in toluene at 425 nm is greater than 56%, wherein the BET surface area is measured according to ASTM D6556-21, the Compressed Oil Uptake is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to described in the specification at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene; and / or (III) carbon black having a BET surface area of 80 m 2 / g to 96 m 2 / g, preferably a BET surface area of 89 m 2 / g to 92 m 2 / g, and the Compressed Oil Uptake is 60 mL / 100g to 69 mL / 100g, preferably the Compressed Oil Uptake is 63 mL / 100g to 65 mL / 100g, Preferably the STSA surface area is 79 m 2 / g to 87 m 2 / g, more preferably the STSA surface area is 82 m 2 / g to 84 m 2 / g, preferably the volatiles are 2.2 wt% to 2.9 wt%, more preferably the volatiles are 2.5 wt% to 2.7 wt%, preferably the transmittance in toluene at 425 nm is greater than 40%, more preferably the transmittance in toluene at 425 nm is greater than 62%, wherein the BET surface area is measured according to ASTM D6556-21, the Compressed Oil Uptake is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to described in the specification at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene; and / or (IV) carbon black having a BET surface area of 120 m 2 / g to 138 m 2 / g, preferably a BET surface area of 127 m 2 / g to 130 m 2 / g, and the Compressed Oil Uptake is 58 mL / 100g to 69 mL / 100g, preferably the Compressed Oil Uptake is 62 mL / 100g to 64 mL / 100g, Preferably the STSA surface area is 82 m 2 / g to 95 m 2 / g, more preferably the STSA surface area is 87 m 2 / g to 89 m 2 / g, preferably the volatiles are 2.6 wt% to 3.2 wt%, more preferably the volatiles are 2.8 wt% to 3.0 wt%, preferably the transmittance in toluene at 425 nm is greater than 60%, more preferably the transmittance in toluene at 425 nm is greater than 80%, wherein the BET surface area is measured according to ASTM D6556-21, the oil absorption under compression is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to described in the specification at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene; and / or (V) carbon black having a BET surface area of 82 m 2 / g to 95 m 2 / g, preferably a BET surface area of 86 m 2 / g to 89 m 2 / g, and the oil absorption under compression is from 59 mL / 100 g to 70 mL / 100 g, preferably the oil absorption under compression is from 63 mL / 100 g to 65 mL / 100 g, Preferably the STSA surface area is 70 m 2 / g to 82 m 2 / g, more preferably the STSA surface area is 76 m 2 / g to 78 m 2 / g, preferably the volatiles are from 1.8 wt% to 2.4 wt%, more preferably the volatiles are from 2.0 wt% to 2.2 wt%, preferably the transmittance in toluene at 425 nm is greater than 60%, more preferably the transmittance in toluene at 425 nm is greater than 80%, wherein the BET surface area is measured according to ASTM D6556-21, the oil absorption under compression is measured according to ASTM D3493-20 using paraffin oil, the STSA surface area is measured according to ASTM D6556-21, wherein the volatiles are measured according to described in the specification at 950 °C for 7 minutes, and the transmittance in toluene at 425 nm is measured according to ASTM D 1618-18 relative to toluene.

12. A composition comprising: (A) an elastomeric polymeric material, and (B) the carbon black obtained according to any one of claims 1 to 10.

13. An article made from or comprising the composition according to claim 12.

14. Use of a particulate carbon-containing feedstock for the manufacture of carbon black in an entrained-flow reactor.

15. A method of adjusting the quenching position in an entrained-flow reactor for the production of carbon black from a particulate carbon-containing feedstock, the method comprising: I) injecting a particulate carbon-containing feedstock into a hot gas stream of an entrained-flow reactor, wherein the temperature of the hot gas stream is at least 800 °C, II) quenching the hot gas stream comprising the produced carbon black, II) measuring the transmittance of the produced carbon black, III) adjusting the quenching position in the entrained-flow reactor until the transmittance of the produced carbon black is at least 20%, preferably at least 30%, more preferably at least 40%, still more preferably at least 60%, most preferably at least 80%, wherein the transmittance in toluene at 425 nm is measured according to ASTM D1618-18 relative to toluene.

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