Feeding and mixing device

Abstract

The invention relates to a feeding and mixing device for particles that can be injected into a reactor, such as an entrained-flow reactor. Thus, the depolymerized particles may be utilized in the reactor. For example, the depolymerization may cause rapid heating of the particles, i.e., facilitating, for example, the formation of carbon black.

Description

Technical Field

[0001] The present invention relates to a feeding and mixing device for pellets that can be fed into a reactor, such as an entrained flow reactor. Thus, deagglomerated pellets can be used in the reactor. For example, deagglomeration allows for rapid heating of the pellets, which, for example, facilitates the formation of carbon black. Background Art

[0002] Using particles in reactors is difficult. Particles tend to agglomerate, resulting in a decrease in specific surface area. However, particles generally need to have a high specific surface area to be utilized in chemical reactions.

[0003] It is particularly desirable to provide an apparatus and method for producing carbon black from particulate or granular carbon-containing feedstock.

[0004] Carbon black has a variety of uses, such as as a reinforcing agent or filler in the rubber and tire industries. Furthermore, carbon black is increasingly being used in other areas, such as as a colorant and in copy toners for photocopiers. These various applications require a variety of carbon black properties, such as particle size, structure, yield, surface area, and tinting strength. The formation of carbon black can be divided into different process steps, including raising the feedstock temperature to the pyrolysis temperature, pyrolysis of the feedstock to unsaturated species (e.g., acetylene and aromatic-containing intermediates), nucleation, surface growth, and aggregation.

[0005] However, the raw materials used to produce carbon black must be converted to gaseous components before pyrolysis. Liquid raw materials are typically used in carbon black production because they evaporate much faster than granular raw materials. While small particles can be used, these particles often form agglomerates. Agglomerated particles heat up more slowly, resulting in inadequate evaporation.

[0006] Therefore, it is desirable to use the particles in a reactor, preferably a furnace reactor. The present invention provides a feeding and mixing device for the particles. The particles are deagglomerated using an accelerated carrier gas flow.

[0007] It has been shown that depolymerized particulate carbonaceous feedstock can be used to produce carbon black. Summary of the Invention

[0008] The objects of the present invention are achieved by a feeding and mixing device for feeding particles into a reactor, the device comprising: (i) a carrier gas channel extending through the feeding and mixing device, (ii) at least one carrier gas inlet in fluid communication with the carrier gas channel, (iii) at least one particle inlet, (iv) a mixing chamber in fluid communication with the at least one particle inlet and the carrier gas inlet, (v) a deaggregation conduit in fluid communication with the mixing chamber, (vi) at least one outlet for entraining the particles fed into the mixing chamber with carrier gas, wherein the at least one outlet is in fluid communication with the deaggregation conduit, and (vii) means for accelerating and injecting the flow of carrier gas into the mixing chamber.

[0009] Furthermore, a reactor system is provided, comprising a reactor and a feeding and mixing device according to the invention, wherein the feeding and mixing device is in fluid communication with the reactor.

[0010] Furthermore, a method for feeding a granular material into a reactor comprises the steps of: (a) deagglomerating and entraining the particles in a carrier gas stream, preferably by using a feeding and mixing device according to the invention, and (b) injecting the carrier gas stream obtained in step (a) comprising the deagglomerated particles into the reactor.

[0011] Furthermore, the feed and mixing device according to the invention serves for deagglomerating particulate, preferably granular, carbonaceous raw materials. BRIEF DESCRIPTION OF THE DRAWINGS

[0012] Figure 1 :Cross-section of furnace reactor

[0013] Figure 2 :Including nozzle (nozzle) feeding and mixing device

[0014] Figure 3 :Laval nozzle for feeding and mixing device

[0015] Figure 4 : Depolymerization pipeline for feeding and mixing device DETAILED DESCRIPTION

[0016] It must be noted that, in the specification and the appended claims, the singular forms "a," "an," and "the" include plural referents unless the context clearly dictates otherwise. Thus, for example, "an oxygen-containing gas" includes mixtures of oxygen-containing gases, "a fuel" includes mixtures of two or more such fuels, and so on.

[0017] Unless otherwise specified, diameter always refers to the inside diameter of an object. For example, the diameter of a tubular conduit refers to the inside diameter of the tubular conduit.

[0018] "Feedstock" refers to the raw material used to produce carbon black. Granular feedstock can be used to produce carbon black. The term "feedstock" or abbreviation used in this invention refers to the granular carbonaceous raw material. The granular feedstock may contain up to 10% by weight of oil (extender oil). For example, rubber particles typically contain up to 10% by weight of oil (extender oil). The oil or extender oil is typically an aliphatic oil or an aromatic oil.

[0019] The expression "hot gas flow" refers to the carrier gas in an entrained flow reactor (e.g., a furnace reactor) that heats the reaction mixture (including the particulate carbonaceous feedstock) to the temperature required for the pyrolysis reaction. For example, the "hot gas flow" is the gas flow after the fuel is burned in a furnace reactor.

[0020] As used herein, "carbon black" refers to a material primarily composed of carbon, e.g., greater than 80%, or greater than 90%, or greater than 95% by weight of carbon, based on its total weight, produced by pyrolysis of a carbonaceous feedstock or by radical driven abstraction of non-carbon atoms in the carbonaceous feedstock. Various industrial processes are known for producing carbon black, such as furnace processes, gas black processes, acetylene black processes, thermal black processes, or lamp black processes. The production of carbon black itself is well known in the art, as summarized, for example, in J.-B. Donnet et al., "Carbon Black: Science and Technology," 2nd ed., and is therefore not described in detail herein.

[0021] The reaction volume of the reactor refers to the volume of the reactor between the injection point of the particulate carbonaceous feedstock and the quenching point.

[0022] The present invention provides a feeding and mixing device for feeding particles into a reactor, comprising: (i) a carrier gas channel extending through the feeding and mixing device, (ii) at least one carrier gas inlet in fluid communication with the carrier gas channel, (iii) at least one particle inlet, (iv) a mixing chamber in fluid communication with the at least one particle inlet and the carrier gas inlet, (v) a deaggregation conduit in fluid communication with the mixing chamber, (vi) at least one outlet for entraining carrier gas with particles fed into the mixing chamber, wherein the at least one outlet is in fluid communication with the deaggregation conduit, and (vii) means for accelerating and injecting a stream of carrier gas into the mixing chamber.

[0023] Figure 2 A preferred feeding and mixing arrangement is shown.

[0024] The carrier gas channel should extend through the feeding and mixing device along a longitudinal axis, and preferably the at least one inlet, the mixing chamber, the depolymerization duct and the outlet are aligned with said longitudinal axis.

[0025] The depolymerization channel is preferably a tubular depolymerization channel.

[0026] The particle inlet should be configured to feed particles into the mixing chamber at an angle relative to the carrier gas jet discharged into the mixing chamber, preferably perpendicular to the carrier gas jet. However, the present invention is not particularly limited to this angle.

[0027] The device for accelerating and injecting the carrier gas flow may include at least one jet nozzle (nozzle). The jet nozzle is configured to accelerate the carrier gas flow. This means that the nozzle (or jet nozzle) is positioned so that the nozzle is convergent in the flow direction, thereby accelerating the gas flow after leaving the nozzle and entering the mixing chamber. In other words, the device for accelerating and injecting the carrier gas flow is preferably convergent in the flow direction extending from the at least one carrier gas inlet toward the at least one outlet.

[0028] The jet nozzle may be a Laval nozzle. Such a Laval nozzle (or nozzle) may include (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 flow of gas. The diverging section increases the diameter of the section. However, the increased diameter of the diverging section is still smaller than the diameter before the converging section. Therefore, the nozzle includes a converging section, a throat, and a diverging section in the following order, and the flow of gas is accelerated.

[0029] The cross-sectional area at each point of the jet nozzle is usually circular or elliptical.

[0030] The jet nozzle may comprise a diverging portion, and the angle of the diverging portion may be 2° to 30°, preferably 3° to 20°, more preferably 4° to 15°, and most preferably 5° to 10°.

[0031] The jet nozzle may include a converging portion, and the maximum inner diameter of the converging portion may be 5 mm to 50 mm, preferably 8 mm to 40 mm, more preferably 10 mm to 30 mm, and most preferably 12 mm to 20 mm.

[0032] The minimum inner diameter of the converging portion, the diverging portion and / or the inner diameter of the throat may 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.

[0033] The minimum inner diameters of the convergent portion, the divergent portion, and the throat inner diameter should be the same. In other words, the convergent portion, the throat, and the divergent portion are generally directly connected to each other.

[0034] The jet nozzle may comprise a diverging portion, and the maximum inner diameter of the diverging portion may 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.

[0035] The minimum inner diameter of the converging portion should be greater than the maximum inner diameter of the converging portion. The difference between the maximum inner diameters of the converging portion and the diverging portion is preferably 5mm to 30mm, preferably 8mm to 20mm, more preferably 9mm to 18mm, and most preferably 10mm to 15mm.

[0036] The maximum inner diameter of the converging portion may be greater than the maximum inner diameter of the diverging portion.

[0037] The distance between the acceleration and injection device and the constant inner diameter pipe can be 2 mm to 20 mm, preferably 2.5 mm to 15 mm, more preferably 3 mm to 10 mm, and most preferably 3.5 mm to 7 mm. This specific distance between these components improves particle disaggregation, as the jet flows directly into the disaggregation pipe. This avoids turbulence and minimizes jet velocity loss.

[0038] The means for accelerating and injecting the carrier gas (or the nozzle) may be positioned such that it protrudes into the cavity of the inlet funnel of the depolymerization conduit.

[0039] The deaggregation conduit typically comprises a conduit having a constant inner diameter, wherein particles collide with each other or with the conduit wall having a constant inner diameter to further deaggregate. The deaggregation conduit may be configured as a diffuser.

[0040] The depolymerization pipeline can include an inlet funnel extending from downstream to upstream, a pipeline having a constant inner diameter, and a diffuser nozzle that diverges in the direction of flow. The diffuser nozzle should continuously increase the inner diameter of the depolymerization pipeline. Therefore, the carrier gas flow is not interrupted, thereby avoiding turbulence. The angle of the diffuser nozzle can be 1° to 30°, preferably 2° to 20°, more preferably 3° to 15°, and most preferably 4° to 8°. The angle of the inlet funnel can be 20° to 80°, preferably 30° to 75°, more preferably 40° to 70°, and most preferably 50° to 65°.

[0041] The longitudinal axis of the depolymerization pipe can be coaxial with the longitudinal axis of the feeding and mixing device. The coaxial arrangement improves the overall acceleration and the depolymerization effect.

[0042] The inner diameter of the tube with a constant inner diameter can be 1 mm to 20 mm, preferably 2 mm to 10 mm, more preferably 3 mm to 7 mm, and most preferably 4 mm to 6 mm. The inner diameter may have an impact on depolymerization. Therefore, the diameter should be selected based on the specific feedstock, preferably based on the mass flow rate.

[0043] The maximum inner diameter of the diffusion nozzle is larger than the inner diameter of the pipe with a constant inner diameter. The maximum inner diameter of the diffusion nozzle should be 5mm to 50mm, preferably 8mm to 40mm, more preferably 10mm to 30mm, and most preferably 12mm to 20mm.

[0044] The diverging nozzle and the converging portion of the jet nozzle may have the same maximum inner diameter.

[0045] The maximum inner diameter of the diffusion nozzle may be 5 mm to 50 mm, preferably 8 mm to 40 mm, more preferably 10 mm to 30 mm, and most preferably 12 mm to 20 mm.

[0046] The length of the pipe having a constant inner diameter can be 3 mm to 500 mm, preferably 5 mm to 200 mm, more preferably 10 mm to 50 mm, and most preferably 13 mm to 30 mm. The length of the pipe can have a beneficial effect on the deagglomeration of the particles (particulate carbonaceous feedstock). Longer pipes generally produce better deagglomeration results.

[0047] The length of the diffusion nozzle may be 10 mm to 300 mm, preferably 20 mm to 200 mm, more preferably 25 mm to 150 mm, most preferably 30 mm to 100 mm.

[0048] The inner diameter of the conduit with a constant inner diameter should be larger than the maximum inner diameter of the outlet of the device for accelerating and injecting the carrier gas flow.

[0049] The means for accelerating and injecting the carrier gas flow, the mixing chamber and the deagglomeration duct should be configured such that the carrier gas jet is discharged in the deagglomeration duct.

[0050] The feeding and mixing device may further comprise at least one hopper located upstream of the at least one particle inlet.

[0051] At least one screw conveyor, such as a screw conveyor, is typically located upstream of the at least one particle inlet. The screw conveyor should be configured to provide a constant amount of particles (or particulate carbonaceous feedstock) to the mixing chamber. Thus, the supply of particles can be controlled by the screw conveyor.

[0052] The particles referred to herein are typically particulate carbonaceous feedstock, and the reactor is typically an entrained flow reactor for making carbon black.

[0053] The feeding and mixing system typically also includes a pressure tank for the pellets, wherein the pressure tank is in fluid communication with the at least one pellet inlet and optionally in fluid communication 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. The two pressure tanks can be connected by a valve.

[0054] A reactor system may be provided, comprising an entrained flow reactor and the above-described feeding and mixing device, wherein the feeding and mixing device is in fluid communication with the reactor. The feeding and mixing device should be connected to a plurality of inlets of the reactor, preferably via injection lances.

[0055] The feeding and mixing device may be in fluid connection with a choke, a combustion chamber and / or a tunnel upstream of the quenching zone of the entrained flow reactor.The reactor may be an entrained flow reactor, preferably a furnace reactor.

[0056] The present invention provides a method for injecting granular material into a reactor, comprising the steps of: (a) deagglomerating and entraining the particles in a carrier gas stream, preferably by using a feeding and mixing device according to the present invention, and (b) injecting the carrier gas stream containing the deagglomerated particles obtained in step (a) into the reactor.

[0057] The process may be a process for producing carbon black, and the particulate material may be a particulate carbonaceous feedstock, and the reactor may be an entrained flow reactor, preferably a furnace reactor, for producing carbon black.

[0058] The particulate carbonaceous feedstock may be injected into the entrained flow reactor through a plurality of inlets, preferably through a plurality of lances.

[0059] The carrier gas flow may be accelerated and flowed through the mixing chamber into the depolymerization conduit.

[0060] Deagglomeration can be accomplished by accelerating the particles in a carrier gas stream and causing the particles to collide with the inner surface of a deagglomeration conduit.

[0061] The carrier gas is typically accelerated to a velocity greater than 1 Ma, preferably 1.01 Ma to 1.7 Ma, more preferably 1.1 Ma to 1.6 Ma, and most preferably 1.2 Ma to 1.5 Ma. However, a flow rate of 0.01 Ma to 3 Ma, preferably 0.1 Ma to 2 Ma, more preferably 0.2 Ma to 1.8 Ma, and most preferably 0.3 Ma to less than 1 Ma is also possible. Ma is the Mach number.

[0062] The particles can be impacted by the carrier gas jet perpendicular to the jet direction.

[0063] The carrier gas stream containing the deagglomerated particles can be injected into the reactor at a pressure of 0.5 to 2 bar, preferably 0.7 to 1.5 bar, more preferably 0.8 to 1.3 bar, and most preferably 0.8 to 1.2 bar. The pressure should be adjusted according to the injection point of the feedstock. For example, the pressure in the combustion chamber is higher than the pressure in the choke, so that the deagglomerated particulate carbonaceous feedstock or the carrier gas containing the deagglomerated particulate carbonaceous feedstock should be injected into the combustion chamber at a higher pressure.

[0064] The carrier gas may further include H2O and / or additives. The carrier gas may contain 1 to 10 volume percent H2O. H2O may prevent particles from reaggregating.

[0065] The feeding and mixing apparatus may be used to deagglomerate particulate, preferably granular, carbonaceous feedstock.

[0066] It is particularly preferred that the particulate carbonaceous feedstock be deagglomerated prior to injection into the reactor. It is believed that the use of deagglomerated particles can reduce evaporation time.

[0067] Accelerating the particulate carbonaceous feedstock can cause the particles to deagglomerate. For example, a carrier gas such as N2 or air can be accelerated and the particles injected into the accelerated carrier gas. In other words, the particulate carbonaceous feedstock can be deagglomerated by placing it into a jet of carrier gas.

[0068] The depolymerization can be carried out in (i) a feeding and mixing device comprising a Laval nozzle.

[0069] Deagglomeration is also achieved by impact of the accelerated particulate carbonaceous feedstock with an object, such as two particles of the particulate feedstock, or by impact of the particles with a surface, such as the inner surface of a deagglomeration conduit.

[0070] The deagglomerated particulate carbon-containing feedstock may be contained in a carrier gas, and the carrier gas may further contain HO and / or additives. HO can prevent reagglomeration of particles in the carrier gas. Therefore, the deagglomerated particulate carbon-containing feedstock should be contained in a carrier gas, and the carrier gas should further contain HO in an amount of 1 to 10% by volume, preferably 2 to 8% by volume, and more preferably 3 to 7% by volume, based on the total volume of the carrier gas containing the deagglomerated particulate carbon-containing feedstock.

[0071] The particulate carbonaceous feedstock and / or the depolymerized carbonaceous feedstock are typically contained or entrained in the carrier gas.

[0072] A method for producing carbon black from a particulate carbonaceous feedstock in an entrained flow reactor having a flow channel along the central longitudinal axis of the reactor, the method may include: (a) providing a hot gas flow, (b) providing a particulate carbonaceous feedstock, and (d) injecting the particulate carbonaceous feedstock into the hot gas flow to form carbon black, wherein the temperature of the hot gas flow is at least 800°C.

[0073] Without wishing to be bound by theory, it is believed that the particulate carbonaceous feedstock heats up at a slower rate than the liquid carbonaceous feedstock, and therefore it is desirable to inject the particulate carbonaceous feedstock into the hot gas stream of the entrained flow reactor at a suitable temperature above 800°C. For example, the temperature of the hot gas stream can be at least 900°C, at least 1000°C, at least 1100°C, at least 1200°C, at least 1300°C, at least 1400°C, at least 1500°C, or at least 1600°C. The minimum required temperature 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.

[0074] The hot gas flow can be obtained by electric preheating, plasma heating, and combustion of fuel and oxygen-containing gas. The hot gas flow can be provided by: (a1) supplying fuel and oxygen-containing gas to a combustion chamber of the reactor, (b2) burning the fuel in the combustion chamber to generate the hot gas flow.

[0075] Therefore, a method for producing carbon black from a particulate carbon-containing feedstock in an entrained flow reactor can be provided, wherein the entrained flow reactor has a flow channel along the central longitudinal axis of the reactor, the method comprising: (a) supplying fuel and an oxygen-containing gas into a combustion chamber of the reactor, (b) burning the fuel in the combustion chamber to produce hot combustion gases, and (d) injecting the particulate carbon-containing feedstock into the hot gas flow to form carbon black, wherein the temperature of the hot combustion gases is at least 800°C.

[0076] As described above, the particles may include a particulate carbonaceous feedstock. The particulate carbonaceous feedstock may include an inert compound, coke, a C and H-containing compound (C,H-containing compounds) and / or carbon black, preferably carbon black and a C and H-containing compound. Typically, the particulate carbonaceous feedstock is a particle and is generally an agglomerated particle. In contrast, a liquid carbonaceous feedstock means that the feedstock is liquid at 20° C. and 1 atmosphere. Preferably, the method for producing carbon black does not utilize a liquid carbonaceous feedstock to produce the carbon black.

[0077] Generally speaking, all raw materials for producing carbon black are pelletized carbon-containing raw materials.

[0078] The particulate carbonaceous feedstock is a feedstock suitable for producing carbon black, ie, new carbon black. Therefore, the particulate carbonaceous feedstock comprises pyrolyzable material.

[0079] Compounds containing carbon and hydrogen (hydrocarbons) can be used to produce carbon black, also known as new carbon black (nCB) or virgin carbon black (vCB). Compounds containing carbon and hydrogen are compounds that contain both carbon and hydrogen. For example, compounds containing carbon and hydrogen are hydrocarbons that may contain heteroatoms such as oxygen or sulfur.

[0080] The particulate carbon-containing feedstock may contain 10 wt% to 100 wt% of C and H-containing compounds, preferably 20 wt% to 99 wt% of carbon and hydrogen-containing compounds, more preferably 30 wt% to 90 wt% of carbon and hydrogen-containing compounds, and most preferably 40 wt% to 70 wt% of carbon and hydrogen-containing compounds, based on the total weight of the particulate carbon-containing feedstock.

[0081] The particulate carbonaceous feedstock may contain an inert compound, and the inert compound may include a metal, a metal compound, silicon, silicon dioxide. The metal may be zinc, sulfur, silicon, calcium, aluminum and / or iron.

[0082] The particulate carbonaceous feedstock may contain 1 wt% to 40 wt% of the inert compound, preferably 3 wt% to 30 wt% of the inert compound, more preferably 4 wt% to 20 wt% of the inert compound, and most preferably 5 wt% to 15 wt% of the inert compound, based on the total weight of the particulate carbonaceous feedstock.

[0083] The granular carbon-containing raw material may also contain carbon black, i.e., recycled carbon black. The carbon black is typically found in tires and, therefore, can be recycled. The granular carbon-containing raw material should contain from 1% to 70% by weight of carbon black, preferably from 5% to 60% by weight, more preferably from 10% to 50% by weight, and most preferably from 15% to 40% by weight, based on the total weight of the granular carbon-containing raw material. Optionally, the granular carbon-containing raw material does not contain recycled carbon black.

[0084] In this context, recycled carbon black means that the carbon black can be recovered in the process. In other words, the carbon black is present in the feedstock but is not produced in the process of the present invention.

[0085] The compound containing C and H is, for example, rubber, plastic and / or biomass-based material. The granular carbon-containing raw material is preferably provided in granular form. Therefore, the granular carbon-containing raw material can include rubber particles, plastic particles and / or biomass-based particles. Therefore, the granular carbon-containing raw material can be a granular rubber raw material, a granular plastic raw material and / or a granular biomass-based raw material. Preferably, the granular carbon-containing raw material includes rubber particles, wherein the rubber particles include carbon black.

[0086] By measuring the C14 content in the raw materials ( 14 The relative amount of C14 atoms to C12 atoms in fossil-based feedstocks compared to biomass-based feedstocks (C14 to C12 ratio / 14 C / 12 Therefore, a fossil-based feedstock refers to a feedstock in which the relative amount of C14 atoms to C12 is lower than the relative amount of C14 atoms to C12 found in nature.

[0087] Preferably, the amount of particulate biomass-based feedstock in the particulate carbon-containing feedstock is 20 wt % to 100 wt %, for example 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 carbon-containing feedstock.

[0088] Preferably, the amount of rubber particles 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.

[0089] Preferably, the amount of granular plastic raw material in the granular carbon-containing raw material is 20 wt % to 100 wt %, based on the total weight of the granular carbon-containing raw material, for example 40 wt % to 100 wt %, 50 wt % to 99 wt %, 60 wt % to 95 wt % or 80 wt % to 90 wt %.

[0090] The pelletized biomass-based carbon black feedstock may include plant-based feedstock, preferably inedible plant-based feedstock and / or plant-based feedstock waste. As used herein, the term "non-edible" refers to materials that are unfit for human consumption. The term "waste" refers to materials that are discarded or disposed of because they are no longer suitable for or useful for their intended purpose (e.g., after use).

[0091] The pelletized biomass-based carbon black feedstock may include wood, grass, cellulose, hemicellulose, lignin, and / or natural rubber.

[0092] The term "timber" as used herein refers to the porous fibrous structure found in the stems and roots of trees and other woody plants. Suitable examples of timber include, but are not limited to, pine, spruce, larch, cypress, ash, hornbeam, birch, alder, beech, oak, pine, chestnut, mulberry or a mixture thereof. The example of suitable grass includes, but is not limited to, cereal grasses, such as corn, wheat, rice, barley or millet; the grass of bamboo and natural grasslands and species cultivated in lawns and pastures. Suitable examples of lignin may include, but are not limited to, lignin and lignin sulfonates removed by the Kraft process.

[0093] The rubber particles may include natural rubber and / or synthetic rubber. The granular carbonaceous raw material may include rubber particles containing carbon black. Natural rubber may be derived from Helvea brasiliensis, guayule, and dandelion. The rubber particles may be tires, cable sheaths, tubes, conveyor belts, shoe soles, hoses, or mixtures thereof.

[0094] The synthetic rubber may include styrene-butadiene rubber, such as emulsion styrene-butadiene rubber (ESBR) and solution styrene-butadiene rubber (SSBR), polybutadiene, polyisoprene, ethylene-propylene-diene rubber (EPDM), ethylene-propylene rubber (EPM), butyl rubber, halogenated butyl rubber, chlorinated polyethylene, chlorosulfonated polyethylene, acrylonitrile-butadiene rubber, hydrogenated acrylonitrile-butadiene rubber, polychloroprene, acrylate rubber, ethylene-vinyl acetate rubber, ethylene-acrylic acid rubber, epichlorohydrin rubber, silicone rubber, fluorosilicone rubber, fluorocarbon rubber, or a mixture or combination of any of the foregoing.

[0095] The plastic particles or granular plastic raw material 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 those derived from toluene diisocyanate (TDI) or methylene diphenyl diisocyanate, and polyolefins such as polypropylene, polyethylene, or polystyrene. Generally speaking, both thermoplastics and thermosetting plastics can be used.

[0096] The plastic particles preferably come from household waste, such as plastic bags, plastic containers, plastic packaging, etc.

[0097] It is desirable to provide the raw material in the form of particles. This can be achieved by grinding to the desired particle size or particle size. For example, tires can be ground to obtain rubber particles as a raw material.

[0098] It is desired that at least 50 wt. %, preferably at least 60 wt. %, more preferably at least 70 wt. %, and most preferably at least 80 wt. % of the particulate carbonaceous feedstock have a particle size of 125 μm to 2 mm, preferably 125 μm to 1 mm, more preferably 250 μm to 1 mm, and most preferably 500 μm to 1000 μm, wherein the particle size is measured according to ASTM D1511-12 (2017).

[0099] It is desired that at least 70 wt. %, preferably at least 80 wt. %, more preferably at least 90 wt. %, and most preferably at least 98 wt. % of the particulate carbonaceous feedstock have a particle size of less than 2 mm, preferably less than 1 mm, more preferably less than 500 μm, and most preferably less than 250 μm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0100] It is desirable that at least 70 wt. %, preferably at least 80 wt. %, more preferably at least 90 wt. %, and most preferably at least 98 wt. % of the particulate carbonaceous feedstock have a particle size of less than 500 μm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0101] It is desired that at least 70 wt. %, preferably at least 80 wt. %, more preferably at least 90 wt. %, and most preferably at least 98 wt. % of the particulate carbonaceous feedstock have a particle size of less than 1 mm, where the particle size is measured according to ASTM D1511-12 (2017).

[0102] It is desired that at least 70 wt. %, preferably at least 80 wt. %, more preferably at least 90 wt. %, and most preferably at least 98 wt. % of the particulate carbonaceous feedstock have a particle size of less than 2 mm, preferably less than 250 μm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0103] It is desired that less than 1 wt. %, preferably at least 0.5 wt. %, more preferably less than 0.1 wt. %, and most preferably less than 0.01 wt. % of the particulate carbonaceous feedstock have a particle size greater than 2 mm, preferably greater than 1 mm, more preferably greater than 500 μm, and most preferably greater than 250 μm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0104] It is particularly preferred that the particle size of the particulate carbonaceous feedstock is less than 2 mm, preferably less than 1 mm, more preferably less than 500 μm, and most preferably less than 250 μm, wherein the particle size is measured according to ASTM D 1511-12 (2017).

[0105] The particle size of the feedstock can be controlled by classifying the particulate carbonaceous feedstock before it is fed into the reactor. Therefore, it is preferred that the particulate carbonaceous feedstock is classified before it is fed into the reactor or into the mixing and feeding unit.

[0106] Classification can be performed by any method known in the art, such as screening or other classification methods. Classification can be performed using a vibrating screen, a rotary screen, a cyclone separator, an elutriation classifier, an air jet screen, and / or a dynamic air classifier. Any combination of the above can be used. Classification can be used to obtain the maximum or minimum desired particle size described in this specification.

[0107] The particle size of the feedstock can be controlled by screening the particulate carbonaceous feedstock before it is injected into the reactor. The sieve sizes described in ASTM D 1511-12 (2017) can be used. For example, a sieve with an opening of 2000 μm, 1000 μm, 500 μm, 250 μm or 125 μm, preferably 500 μm, 250 μm or 125 μm can be used. In addition, the size of the opening of the sieve can restrain particles with a size greater than 2000 μm, greater than 1000 μm, greater than 500 μm, greater than 250 μm or greater than 125 μm, preferably greater than 500 μm, greater than 250 μm or greater than 125 μm.

[0108] Not more than 10 wt. %, preferably not more than 5 wt. %, more preferably not more than 4 wt. %, and most preferably not 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, and most preferably greater than 0.5 mm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0109] Not more than 10 wt. %, preferably not more than 5 wt. %, more preferably not more than 4 wt. %, and most preferably not more than 2 wt. % of the particulate carbonaceous feedstock should have a particle size of less than 150 μm, preferably less than 125 μm, more preferably less than 110 μm, and most preferably less than 100 μm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0110] The particle size of all particles of the granular carbonaceous raw material should not be greater than 1 mm, preferably should not be greater than 500 μm, more preferably should not be greater than 250 μm, and most preferably should not be greater than 125 μm, where the particle size is measured according to ASTM D 1511-12 (2017).

[0111] The particle size distribution of the particulate carbonaceous feedstock can be measured according to ASTM D 1511-12 (2017), and (a) a No. 10 sieve retains 1 wt % to 0 to 10 wt %, preferably 1 wt % to 8 wt %, more preferably 1 wt % to 5 wt %, and most preferably 1 wt % to 3 wt % of the particulate carbonaceous feedstock, and / or (b) a No. 18 sieve retains 1 wt % to 25 wt %, preferably 2 wt % to 20 wt %, more preferably 4 wt % to 15 wt %, and most preferably 5 wt % to 12 wt % of the particulate carbonaceous feedstock, and / or (c) a No. 35 sieve retains 10 wt % to 80 wt %, preferably 15 wt % to 70 wt %, more preferably 20 wt % to 60 wt %, and most preferably 25 wt % to 55 wt %. % of the particulate carbon-containing feedstock, and / or (d) a No. 60 sieve retains 5 to 70 wt. %, preferably 10 to 60 wt. %, more preferably 15 to 50 wt. %, and most preferably 20 to 45 wt. % of the particulate carbon-containing feedstock, and / or (e) a No. 120 sieve retains 1 to 80 wt. %, preferably 7 to 70 wt. %, more preferably 5 to 60 wt. %, and most preferably 7 to 50 wt. % of the particulate carbon-containing feedstock, and / or (f) the bottom receiving tray contains less than 4 wt. %, preferably less than 3 wt. %, more preferably 0 to 2 wt. %, and most preferably 0.01 to 1 wt. % of the particulate carbon-containing feedstock. It is advisable to select the desired range independently for each sieve.

[0112] The 50 wt% cumulative particle size of the particulate carbonaceous feedstock should be 100 μm to 4 mm, preferably 100 μm to 3 mm, more preferably 100 μm to 2 mm, and most preferably 100 μm to 500 μm, wherein the 50 wt% cumulative particle size is measured according to ASTM D 1511-12 (2017). The 50 wt% cumulative particle size can be interpolated using standard techniques known in the art. It is particularly preferred to use the Rosin-Rammler-Sperling-Bennett distribution (RRSB distribution) to interpolate the 50 wt% cumulative particle size.

[0113] The weight average particle size Dw50 of the particulate carbonaceous raw material can be 100 μm to 4 mm, preferably 100 μm to 3 mm, more preferably 100 μm to 2 mm, and most preferably 100 μm to 500 μm, wherein the weight average particle size Dw50 is measured according to ASTM D 1511-12 (2017).

[0114] The particle size distribution Dw10 of the particulate carbonaceous raw material can be 100μm to 250μm, preferably 110μm to 220μm, more preferably 120μm to 210μm, and most preferably 130μm to 200μm, wherein the particle size distribution Dw10 is measured according to ASTM D 1511-12 (2017).

[0115] The particle size distribution Dw90 of the particulate carbonaceous raw material can be 400μm to 4mm, preferably 500μm to 3mm, more preferably 600μm to 2mm, and most preferably 700μm to 500μm, wherein the particle size distribution Dw90 is measured according to ASTM D 1511-12 (2017).

[0116] The particle size distribution span (Dw90-Dw10) / Dw50 of the particulate carbonaceous raw material can be 0.4 to 2.5, preferably 0.7 to 2, more preferably 1 to 1.8, and most preferably 1.2 to 1.7, where the particle size distribution Dw10, Dw50 and Dw90 are measured according to ASTMD 1511-12 (2017).

[0117] Dw50, Dw10, and Dw90 can be interpolated using standard techniques known in the art. In particular, it is preferred to use the Rosin-Rammler-Sperling-Bennett distribution (RRSB distribution) to interpolate Dw50, Dw10, and Dw90.

[0118] Particle or granulate size affects the heating rate (temperature ramp rate) of the feedstock in the reactor. Smaller particles have a greater surface area and, therefore, a faster heating rate. A faster heating rate is beneficial so that the granular feedstock can evaporate and then pyrolyze. It is believed that the pyrolysis rate of granular feedstock is significantly faster than the evaporation rate. The heating rate can also be increased by increasing the temperature of the hot gas stream.

[0119] The carbon black (e.g., including rCB (recycled carbon black)) and / or the particulate carbonaceous feedstock produced as described above may have a pMC (percent of modern carbon) greater than 1% as measured by ASTM D6866-20 Method B (AMS). 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, or 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. For each sample, calculate 14 C / 13 C ratio and compare it with the measured value of oxalic acid II standard (Oxalic Acid II standard) (NIST-4990C). The measured value (pMC) is corrected by d13C measured using an isotope ratio mass spectrometer (IRMS). The carbon black may have a pMC (modern carbon percentage) of 5% or more, preferably 10% or more, particularly preferably 15% or more, more preferably 50% or more, even more preferably 85% or more, and most preferably 90% or more, as measured according to ASTM D6866-20 Method B (AMS). The carbon black may have a pMC (modern carbon percentage) of 100%, as measured according to ASTM D6866-20 Method B (AMS).

[0120] The carbon black obtained generally includes recycled carbon black and new carbon black. If the particulate carbonaceous feedstock includes carbon black, recycled carbon black is generally obtained. New carbon black is obtained by pyrolysis, i.e. the process described above.

[0121] The mass flow of the feedstock should be adjusted so that the feedstock is heated uniformly. The particulate carbonaceous feedstock should be injected into the reactor at a mass flow rate of 2 to 50 kg / h per 130 L of reactor volume, preferably 5 to 40 kg / h per 130 L of reactor volume, more preferably 8 to 30 kg / h per 130 L of reactor volume, and most preferably 10 to 20 kg / h per 130 L of reactor volume.

[0122] The fuel may comprise gaseous or liquid hydrocarbons, preferably natural gas, fuel oil or H2.

[0123] Hydrogen can be used as a carrier gas and / or fuel for the production of carbon black. Hydrogen is preferably used as both a carrier gas and a fuel for the production of carbon black. If the molar excess of hydrogen relative to oxygen is present in the combustion mixture, hydrogen will be used as a carrier gas. Therefore, hydrogen should be present in the hot combustion gases and the hot reaction mixture.

[0124] The temperature of the hot gas stream should be 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.

[0125] The hot gas stream can be obtained by electrical preheating, plasma, and combustion of fuel and oxygen-containing gas. The combustion of fuel and oxygen-containing gas is preferably carried out in a furnace reactor. However, as mentioned above, other methods can also be used to provide the required temperature of the hot gas stream.

[0126] The reactor can be an entrained flow reactor. 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 includes a combustion chamber, a choke, and a tunnel comprising a quenching device from upstream to downstream (flow direction). These components define a flow channel along the central longitudinal axis of the reactor for hot gas flow, such as hot combustion gases. Therefore, each component should remain fluidically connected, particularly along the central longitudinal axis of the reactor.

[0127] The tubular conduit may be connected to the combustion chamber to supply the oxygen-containing gas required for the combustion of the fuel (or fuel). The tubular conduit may also be arranged along the central longitudinal axis of the reactor so that the oxygen-containing gas is replenished along the aforementioned flow path. In addition, the reactor may include a fuel injection device for injecting fuel into the combustion chamber.

[0128] Fuel is typically supplied to the combustion chamber using a fuel lance. The combustion chamber may be connected to a tubular conduit in a downstream to upstream direction, allowing oxygen-containing gas to be supplied to the combustion chamber. The combustion chamber is arranged along the central longitudinal axis of the reactor.

[0129] The combustion chamber is preferably formed of an inner refractory lining covered by a gas-tight cover layer, such as a metal cover layer. The materials forming the refractory material and the outer lining may be materials commonly used in the art, such as A 32-cm castable refractory material with a 70% alumina (Al2O3) content and a melting point of approximately 1870°C can also be used. Alternatively, a brick refractory material such as RUBY SR (sold by Harrison-Walker Refractories, Inc., Pittsburgh, Pennsylvania) can be used. This brick refractory material contains 84.5% alumina and 9.8% chromium oxide (Cr2O3) and has a melting point of approximately 2050°C. The shell or liner is preferably made of carbon steel, except for all piping that comes into contact with hot process air. In these areas, the piping is made of 316 stainless steel.

[0130] The combustion chamber is preferably designed as a cylinder. A constricting section (throttling portion) may be provided downstream of the combustion chamber. The constricting section has a gradually tapering channel that converges from upstream to downstream. Preferably, these constrictions are in the form of frustoconical channels. The combustion chamber may also have a tapered structure that tapers from downstream to upstream. Thus, the combustion chamber may include a region that tapers toward the reaction chamber and / or toward the tubular conduit.

[0131] Typically, the oxygen-containing gas is preheated to 200°C to 1600°C, preferably 350°C to 1400°C, more preferably 500°C to 1200°C, most preferably 450°C to 950°C.

[0132] Typically, the fuel is preheated to a temperature of 50°C to 750°C, preferably 100°C to 700°C, more preferably 300°C to 700°C, most preferably 450°C to 650°C.

[0133] Preheating of the oxygen-containing gas and the fuel can be performed electrically or by heat exchangers. Preheating the hydrogen and / or the oxygen-containing gas is particularly preferred since less energy is required, e.g. from combustion of the fuel.

[0134] Another benefit of preheating is that the amount of oxygen-containing gas required is lower and the hot combustion mixture as well as the hot reaction mixture contains less water (H2O). Water affects the surface properties of the produced carbon black.

[0135] The tunnel is typically connected to the combustion chamber so that the hot combustion gases obtained in the combustion chamber can flow into the tunnel. The tunnel may be arranged along the central longitudinal axis of the reactor. The diameter of the reaction chamber may be larger than the diameter of the combustion chamber's constriction to allow the hot combustion gases to expand. The expansion section is preferably cylindrical and communicates with the combustion chamber, preferably with the constriction (choke) of the combustion chamber.

[0136] The particulate carbonaceous feedstock can be injected into the combustion chamber, the throttling section and / or the passage of the furnace reactor. The particulate carbonaceous feedstock is usually injected into the throttling section (contraction section).

[0137] If the particulate carbonaceous feedstock is injected into, for example, a combustion chamber, the particulate carbonaceous feedstock or the carrier gas containing it should be at a desired pressure. This means that the pressure of the particulate carbonaceous feedstock or the carrier gas containing it should be higher than the pressure within the combustion chamber. Therefore, suitable feeding and mixing equipment configured to operate under pressurized conditions should be used.

[0138] The particulate carbonaceous feedstock should be injected through a plurality of inlets, preferably radially and perpendicularly to the central longitudinal axis of the reactor.

[0139] The O2 concentration in the hot gas stream is less than 5% by volume, preferably less than 4% by volume, more preferably 0.01% to 3% by volume, and most preferably 0.1% to 2% by volume.

[0140] The granular carbonaceous feedstock can be injected into the reactor via a feedstock injection device. The feedstock injection device can include multiple injection nozzles or spray guns, which are preferably arranged circumferentially with respect to the central longitudinal axis. This circumferential arrangement further improves the uniformity of the carbon black because the carbon black feedstock can be evenly mixed with the hot combustion gases. The granular carbonaceous feedstock can be introduced into the reactor by various means.

[0141] For example, axially extending feedstock lances and radially extending feedstock injectors having nozzles capable of producing various cone sprays (eg, 15, 30, 45, and 60 degree cone spray angles) may be employed.

[0142] In order to produce the desired carbon black properties, shutoff valves may be provided on the radially extending feedstock injectors to allow feedstock to be introduced only through certain feedstock injectors, or to vary the flow rate of feedstock flowing in the injectors.

[0143] The raw material injection device is preferably connected to the feeding and mixing device. It is expected that one feeding and mixing device can supply multiple raw material inlets. However, more than one feeding and mixing device can also be used.

[0144] The channel may also include a device for injecting a quenching medium into the flow channel along the central longitudinal axis of the reactor, the device being downstream of the injection of the carbon black feedstock relative to the flow direction. Optionally, the quenching device may be a quench boiler or a heat exchanger.

[0145] The channel may include a device for injecting a quenching medium into the flow channel along the central longitudinal axis of the reactor. The quenching medium injection device is located after (downstream of) the carbon black feedstock injection device relative to the flow direction. The quenching medium is typically H2O.

[0146] The distance between the raw material injection device and the quenching medium injection device (first quenching medium injection device) may be 150 mm to 80,000 mm, preferably 900 mm to 50,000 mm, more preferably 1,500 mm to 30,000 mm, and most preferably 2,500 mm to 20,000 mm.

[0147] The quenching medium injection device can extend into the channel. For example, a cooling fluid conduit or multiple radial cooling fluid conduits can be used. The quenching medium (e.g., a coolant (e.g., water)) is injected into the channel to stop the carbon black reaction at the appropriate time and location.

[0148] The reactor can also include a tubular conduit for supplying oxygen-containing gas to the combustion chamber. Oxygen-containing gas (containing O gas or containing O gas mixture) can be air, oxygen-enriched air, other oxygen-containing gases and / or pure oxygen. Therefore, tubular conduit can be connected with the combustion chamber so that oxygen-containing gas can flow through the tubular conduit in the combustion chamber. Tubular conduit can be arranged along the central longitudinal axis of the reactor. The central longitudinal axis of the desired tubular conduit is coaxial with the central longitudinal axis of the reactor. Therefore, tubular conduit can be arranged coaxially along the central longitudinal axis of the reactor. The weight percent of the oxygen present in the oxygen-containing gas should be 20 weight % to 100 weight %, preferably 50 weight % to 99 weight %, more preferably 60 weight % to 95 weight %, most preferably 70 weight % to 90 weight %, wherein weight percent is based on the gross weight of the oxygen-containing gas.

[0149] The tubular conduit may have a cylindrical shape extending straight along the central longitudinal axis of the reactor without curvatures.

[0150] The inner diameter of the tubular pipe for supplying oxygen-containing gas may be 5 cm to 3 m, for example 10 cm to 3 m, 20 cm to 3 m, 9 cm to 2.5 m, 13 cm to 1.5 m, 0.1 m to 2 m, 20 cm to 1 m, 30 cm to 1.5 m, 15 cm to 60 cm or 15 cm to 90 cm.

[0151] Preferably, the inner diameter of the entire tubular conduit is constant, but the tubular conduit may also have two different sections connected to an inflow funnel that reduces the inner diameter of the tubular conduit toward the flow direction (i.e., toward the combustion chamber). Thus, the tubular conduit may have a first section having a first inner diameter and a second section having a second inner diameter that is smaller than the first inner diameter. The first inner diameter may be in the range of 5 cm to 3 m, such as 20 cm to 3 m, 9 cm to 2.5 m, 13 cm to 1.5 m, 0.1 m to 2 m, 20 cm to 1 m, 30 cm to 1.5 m, 15 cm to 60 cm, or 15 cm to 90 cm, and the second inner diameter may be in the range of 5 cm to 3 m, such as 20 cm to 3 m, 9 cm to 2.5 m, 13 cm to 1.5 m, 0.1 m to 2 m, 20 cm to 1 m, 30 cm to 1.5 m, 15 cm to 60 cm, or 15 cm to 90 cm.

[0152] 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 or fuel oil, or H2) can be configured in various ways. For example, the injection means can be disposed at the end of a tubular conduit connected to the combustion chamber. For example, the injection means is a tubular injection pipe arranged circumferentially relative to the central longitudinal axis of the tubular conduit such that the fuel is injected at an angle substantially perpendicular to the flow direction of the oxygen-containing gas.

[0153] However, in addition to the fuel lance, a plurality of fuel injection devices may also be provided. For example, at the end of the tubular conduit, the additional fuel injection device is arranged rotationally symmetrically with respect to the central longitudinal axis of the tubular conduit.

[0154] The oxygen-containing gas is typically supplied in an amount that supplies an excess of oxygen relative to the amount of oxygen required for complete combustion of the fuel, and / or wherein the oxygen-containing gas is supplied in an amount 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, and most preferably 0.7 to 1. The k value is defined by the ratio of the stoichiometric amount of O2 required for complete stoichiometric combustion of the fuel to the amount of O2 supplied.

[0155] The flow rate ratio of the fuel and oxygen-containing gas can be adjusted to produce high temperatures and is usually close to the stoichiometric ratio. The above ratio must be adjusted to prevent the refractory from melting. The range of oxygen-containing flow is quite wide, for example, from about 1000 Nm 3 / h to a low of about 100km / h 3 / h, such as 1000Nm 3 / h to 100km 3 / h、1000Nm 3 / h to 10km 3 / h、2000Nm 3 / h to 3000Nm 3 / h, or 1000Nm 3 / h to 2000Nm 3 However, the present invention is not limited to these dimensions; for larger reactors, higher air flow rates are required, while for smaller reactors, lower air flow rates are required.

[0156] The desired temperature of the hot gas stream can also be achieved by heating the gas stream with plasma.The gas stream can be preheated as described above.

[0157] A plasma torch can provide the plasma for the above-mentioned heating. A plasma torch design is described in WO1993 / 012633A1. However, any method known in the art for generating plasma can be used. Plasma can be formed by a plasma carrier gas heated by an arc burning between electrodes. The temperature of the plasma zone is as high as 3000°C to 20,000°C, and plasma treatment can be performed in this area. The plasma carrier gas can be oxygen or hydrogen. Hydrogen is particularly preferably used as the plasma carrier gas.

[0158] Microwave plasma can also provide plasma for the above-mentioned treatment. For example, a microwave generator can be used to provide microwave radiation in the reaction chamber. Microwave radiation of 1 GHz to 300 GHz can be used. Alternatively, a radio frequency power supply (RF generator) can also be used to generate the plasma.

[0159] The residence time between the time when the particulate carbonaceous raw material is injected into the reactor and the time when the product mixture is quenched should be 150ms to 4s, preferably 200ms to 3s, more preferably 250 to 2s, and most preferably 250ms to 1s. The residence time of the particulate carbonaceous raw material refers to the time when the particulate carbonaceous raw material evaporates and pyrolyzes. The quenching of the product mixture stops the pyrolysis of the particulate carbonaceous raw material. The heating rate of the particulate carbonaceous raw material is lower than that of the liquid raw material, so the evaporation and pyrolysis of the particulate carbonaceous raw material usually require more time.

[0160] The residence time of the particulate carbonaceous feedstock should be 150 ms to 4 s, preferably 200 ms to 3 s, more preferably 250 to 2 s, and most preferably 250 ms to 1 s, wherein the residence time is calculated according to equation (1);

[0161]

[0162] Equation (1),

[0163] where t r is the residence time, V is the volume of the reaction volume (in m 3 Q is the volumetric flow rate (in m 3 *s -1 as units).

[0164] The volume flow rate is the volume of fluid flowing per second after the granular carbonaceous raw material is injected into the hot gas flow. The volume of the fluid is preferably calculated according to equation (2) based on the ideal gas law.

[0165]

[0166] Equation (2),

[0167] Q is the volume flow rate of the fluid (unit is m 3 *s -1 ), It is the sum of the molar flow rates of gaseous substances N2, CO2, CO, H2O, and volatile components (unit: mol*s -1 ), R is the gas constant, which is 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 alternatively calculated using 103125 Pa. and the content of substances, all substances are considered to be gaseous (including particulate carbonaceous raw materials). Volatiles are the volatiles of particulate carbonaceous raw materials determined according to ASTM D4530-15 (2020). For the molecular weight of volatiles, 198 g / mol can be used. The composition calculation of the hot gas flow takes into account the complete combustion of the fuel. For the remaining oxygen, it is assumed that the oxygen reacts with the carbonaceous substances, assuming that one O2 produces one H2O and one CO. The calculation takes into account the fluid after the particulate carbonaceous raw material is injected into the hot gas flow (for volume flow calculation), and the carbonaceous part of the raw material is completely in the gaseous state. Non-gaseous materials are not considered. In addition, the pyrolysis of the carbonaceous part in the raw material is not taken into account in the calculation. Calculation examples are given in this manual, which can be applied to the specific method of manufacturing carbon black.

[0168] The reaction volume of the reactor is the volume of the reactor between the injection point of the particulate carbonaceous feedstock and the quenching point.

[0169] The residence time is selected to ensure complete pyrolysis of C and H-containing species in the particulate carbonaceous feedstock.

[0170] The absolute temperature used to calculate the volume flow rate can be measured directly in the reactor. Specifically, the temperature is measured directly after the feedstock is injected into the reactor, for example, 50 mm after the feedstock is injected. For example, the temperature can be measured using a pyrometer.

[0171] Alternatively, the absolute temperature T (used to calculate the volumetric flow rate) can be calculated as follows. This calculation takes into account the combustion of the fuel in the furnace reactor. This process involves the combustion of the fuel and the heating of the rubber particles to the reaction temperature. Burning residual oxygen does not result in complete combustion. Therefore, it can be assumed that, depending on the C / H ratio of the feedstock, CO and HO will be generated with the same CO / H2O ratio.

[0172] The reaction temperature can be controlled by energy balance.

[0173]

[0174] Calculate according to equation (3).

[0175] The mass flow rate of fuel is expressed in m F Indicates that h F is the thermal enthalpy difference between the temperature and pressure at the fuel combustion chamber inlet and the fuel reference conditions (T = 25 ° C, P = 101325 Pa), m A is the mass flow rate of the inert substance, h A ΔH is the thermal specific enthalpy difference between the inert material A at 25°C and 1.01325 bar and the conditions (TA, PA) under which the inert material is introduced into the combustion chamber. The amount of inert material is expressed in K. Inert materials are substances that do not change in an ideal process. Examples of these inert materials are nitrogen, carbon black, minerals, and water. uF The difference in oxygen enthalpy between the feed condition and the reference condition (T = 298.15K, P = 101325Pa) is expressed as The oxygen mass flow rate is expressed as The specific thermal enthalpy difference between the reaction product i under the conditions of reaction temperature T, P = 101325Pa and the reference conditions (T = 298.15K, P = 101325Pa) is expressed as h i The corresponding mass flow rate is expressed in mp i The lower heating value of the compound is expressed as H ui If the granular raw material is transported to the reactor with the gas flow, the gas mass flow rate is expressed as m T The enthalpy difference between the conditions at the reactor inlet and the reference conditions (T = 25 ° C, P = 103125 Pa) is expressed as (h T Indicates that H uT is the corresponding lower specific heating value. Loss Heat losses are taken into account. The mass flow rate of the hydrocarbon part of the granular raw material is expressed in m R Indicates that m R =m s (1-w-Conradson) calculation, the mass flow rate of granular raw materials is expressed in m s The thermal enthalpy difference between the hydrocarbon in the entry state and the reference state (T = 25 ° C, P = 101325 Pa) is represented by h R The corresponding lower heating value is given by H uR given.

[0176] The lower calorific value is determined according to DIN 5499 and DIN 51857. If the gas is not reported in DIN 51857, the calorific value can be determined from the heat of formation. These values ​​can be found in "Properties of Gases and Liquids", NIST DataBook, etc. Based on substance C x H y S z O w Assumptions of complete oxidation and gaseous water as a reaction product,

[0177]

[0178] Equation (4)

[0179] Where A is unoxidized substance. f It is the substance A that exists in the form of A in the combustion products. Therefore, p = fe.

[0180] The calorific value is

[0181]

[0182] Equation (5).

[0183] If the reference temperature of the heat of formation of substance i is different from 298.15K, the heat can be calculated using the molar heat capacity

[0184]

[0185] Equation (6).

[0186] Molar heat capacity can be found using the same textbooks, such as Properties of Gases and Liquids, NIST Data Book.

[0187] If the fuel is composed of more than one substance, the lower heating value can be composed of

[0188]

[0189] Determine Equation (7).

[0190] The mass fraction of component I is expressed as ξ i The lower heating value of component i is expressed as ΔH u,i The number of types of substances in the fuel is represented by P.

[0191] The enthalpy difference of a fuel containing more than one species can be given by

[0192]

[0193] Calculate Equation (8).

[0194] The average molecular weight of the fuel is given by

[0195]

[0196] Determine Equation (9).

[0197] M i is the molecular weight of substance i.

[0198] If the composition is unknown, the lower heating value is determined using a calorimeter. If the fuel is solid or liquid, the lower heating value is determined according to DIN 51900. As can be seen from the experimental results, the water content is measured according to ASTM D4928-12 (2018), and the sulfur and hydrogen contents are measured according to the methods described in the examples.

[0199] The enthalpy difference between the flue gas at T = 298.15K and the flame temperature is given by

[0200]

[0201] Determine by equation (10).

[0202] The number of species in the product gas stream is represented by N, and the average molecular weight of the flue gas is represented by M. Gas The average molecular weight is represented by

[0203]

[0204] Determine by equation (11).

[0205] The lower heating value of the inert materials in the product stream was set to 0 J / mol.

[0206] To determine the lower heating value of hydrocarbon-containing materials in pelletized feedstock, the water content must be determined according to ASTM D4928-12 (2018), and the microconradson content must be determined according to ASTM D4530-15 (2020). In addition, the ultimate analysis of the pelletized feedstock must be measured according to ASTM D3176-15 (2016), and the gross calorific value must be measured according to ASTM D 4809:2018.

[0207] The lower calorific value of the granular raw materials is

[0208] H us =(H os -(w s +9h s )Δ vap h 水 )1 / (1-w)

[0209] calculate.

[0210] Alternatively, the lower heating value of Conradson residue can be determined by measuring the gross heating value and hydrogen content of the Conradson residue using the same equation. The moisture content of Conradson residue is zero. The lower heating value of the hydrocarbon-containing pelletized feedstock is given by

[0211] H uR =H us (1-w)-H uConradson Conradson) / (1-w-Conradson)

[0212] Sure.

[0213] The C / H ratio of the hydrocarbon fraction can be obtained by elemental analysis of the pelletized raw material and elemental analysis of Conradson carbon residue.

[0214]

[0215] The molar enthalpy difference of water can be calculated by

[0216]

[0217] Determine by equation (12).

[0218] For CO2, this can be done by

[0219]

[0220] Determine by equation (13).

[0221] For SO2,

[0222]

[0223] Equation (14) is obtained.

[0224] For N2,

[0225]

[0226] Equation (15) is obtained.

[0227] For O2,

[0228]

[0229] Equation (16) is obtained.

[0230] For CO,

[0231]

[0232] Equation (17) is obtained.

[0233] The lower heating value of CO is For gaseous rubber products,

[0234] Equation (18) is obtained.

[0235] For granular rubber, we obtain

[0236] h 橡胶,s =1960J / kgK(T-298.15K)

[0237] Equation (19).

[0238] For Conradson carbon residue,

[0239]

[0240] Equation (20).

[0241] Example Calculation

[0242] Combustion of methane entering the combustion chamber at a pressure of 3 bar and a temperature of T = 290K

[0243] The standard volume flow rate of methane at a pressure of 101325Pa and a temperature of T = 273.15K is 13Nm 3 / h (STP); When the temperature is T = 673.15K and the pressure is 1.2 bar, the standard volume flow rate of nitrogen (converted to standard conditions: pressure 101325Pa, temperature 273.15K) is 118.5Nm 3 / h (STP); the standard flow rate of oxygen is 31.5Nm 3 / h (STP), reference standard temperature T = 273.15K, standard pressure P = 101325Pa.

[0244] In the throttle section, rubber particles were added at a mass flow rate of 20 kg / h into the system at a temperature of 20° C. and a pressure of 1 bar.

[0245] At T = 298.15K and P = 101325Pa, the lower heating value of methane according to DIN 51857 is 802.6MJ / kmol. In "Properties of Gases and liquids", the heat capacity of methane is obtained as

[0246] 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)

[0247] Equation (22).

[0248] Therefore, through

[0249]

[0250] Equation (23) yields h_f.

[0251] The temperature of the fuel feed is denoted by T, which is T=290K in this example, and the reference temperature for the calorific value is T0=298.15K.

[0252] The enthalpy difference between the inert gas nitrogen at T = 298.15 K and the feed temperature can be determined by equation (4). For oxygen, we can determine the enthalpy difference by equation (15).

[0253] Heat loss occurs in the reactor shell and can be calculated based on the measured shell temperature according to VDI Calculate heat transfer. Heat transfer should include radiation and convection / natural convection.

[0254] Calculation of mass flow rate of compounds in the reaction zone

[0255] In equation (4), x=1, y=4 and z=0, w=0, p=0. Therefore, we have 13Nm 3 / h of methane to obtain 13Nm 3 / h of carbon dioxide and 26Nm 3 / h of water. The residual oxygen content is determined by subtracting the oxygen flow in the form of CO2 and H2O (and SO2 if the fuel contains sulfur). For gaseous substances, the conversion between mass flow rate and standard volume flow rate is determined by

[0256]

[0257] Equation (24) is carried out,

[0258] T0 is 273.15K, P 0 It is 101325Pa.

[0259] Therefore, we obtain the remaining oxygen flow

[0260]

[0261] Equation (25).

[0262] Assume that the residual oxygen is converted by hydrogen and carbon of the rubber part of the pellet according to the atomic H / C ratio of the rubber part. Assuming an H / C ratio of 2, we obtain one H2O and one CO. Therefore, we must add the following 5.5 Nm to the already calculated water flow rate: 3 / h of H2O flow, a total of 31.5Nm 3 / h of H2O and 5.5Nm 3 / h of CO. Rubber particles pass 8Nm 3 / h of nitrogen is delivered to the reactor.

[0263] Converting these gas flow rates to mass flow rates using the above equations yields:

[0264]

[0265] The rubber mass flow rate in the gas phase is calculated by subtracting the inert material from the total rubber particle flow rate and then subtracting the burned rubber mass flow rate.

[0266]

[0267] Equation (26).

[0268] Treating Conradson carbon residue as an inert material, it can be calculated using the following formula

[0269]

[0270] Equation (27).

[0271] Heat loss calculation

[0272] Heat flux can be measured by

[0273]

[0274] Calculated by equation (28).

[0275] In the case of natural convection, α is calculated from the Nusselt number (Nu), which is a function of the Rayleigh number (Ra) and the Prandtl number (Pr).

[0276]

[0277] Equation (29)

[0278] use

[0279]

[0280] Equation (30).

[0281] Rayleigh number through

[0282]

[0283] Calculated by equation (31).

[0284] Taking all of this into account in the energy balance, we obtain

[0285]

[0286] Equation (32).

[0287] The external area of ​​the reactor is 15.9m 2 . Therefore, for the given example, we obtain 1629°C. The reaction volume is 0.162m 3 The volume flow rate of all substances except mConradson is 1236m 3 / h. Therefore, we obtain the residence time of 0.38 seconds according to the following equation (1):

[0288]

[0289] In the last equation, the reactor volume is represented by V and the volumetric flow rate of all substances except the Conradson carbon is represented by Q. In this example, all substances except the Conradson carbon are rubber, residual (Res) CO2COH2O N2.

[0290] Typically, the residence time is selected so that the C and H-containing species in the particulate carbonaceous feedstock are completely pyrolyzed.

[0291] The formation of carbon black is generally terminated by quenching the hot gas stream.Thus, the method for producing carbon black may further comprise (e) quenching the hot gas stream after injection according to step (d).

[0292] The transmittance can indicate whether the residence time of the feedstock is sufficient to completely pyrolyze, for example, C- and H-containing species in the feedstock. Thus, the hot gas stream (e) should be quenched when the transmittance of the obtained carbon black at 425 nm 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 with toluene according to ASTM D1618-18.

[0293] The transmittance of the carbon black produced at 425 nm can be measured and the position of the quench 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%, even more preferably at least 60%, and most preferably at least 80%, wherein the transmittance at 425 nm in toluene is measured using toluene according to ASTM D 1618-18.

[0294] The quench position in the entrained flow reactor can be selected so that the carbon black produced has a transmittance at 425 nm of 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 for toluene according to ASTM D 1618-18.

[0295] Carbon black is included in many polymer compositions, for example, to modify their color, mechanical, electrical, and / or processing properties. For example, carbon black is often added to rubber compositions used in the manufacture of tires or their components to impart electrically dissipative properties to the insulating matrix. Furthermore, carbon black additives can affect mechanical and elastic properties, such as stiffness, wear resistance, and hysteresis, which significantly impact the final tire's performance, such as its rolling resistance and durability.

[0296] The present invention will now be described with reference to the accompanying drawings, but the drawings do not limit the scope and limits of the present invention. The description provided is purely for example and illustration. However, the specific features illustrated in the drawings can be used to further limit the scope of the present invention and the claims.

[0297] Figure 1A furnace reactor (100) is shown, which includes a combustion chamber (101), a choke (102) and a channel (103). The reactor has an inner lining (106) and an outer lining (105). The combustion chamber (101) includes a fuel injection device (101b) and an oxygen-containing gas injection device (101a). In the figure, the oxygen-containing gas is injected tangentially or radially into the combustion chamber (101) through the oxygen-containing gas device (101a), and the fuel is injected axially into the combustion chamber (101) through the fuel injection device (101b). The oxygen-containing gas is preferably preheated to the temperature described in this specification. The temperature of the hot gas flow can be adjusted by preheating the oxygen-containing gas. Optionally, the fuel can be preheated. In the combustion chamber (101), the fuel is burned in the presence of the oxygen-containing gas. After combustion, the temperature of the hot carrier gas is higher than 800°C, so that the particulate carbon-containing raw material reaches the temperature required for pyrolysis. The granular carbonaceous feedstock can be injected directly into the combustion chamber (101), the throttle (102) or the channel (103). The granular carbonaceous feedstock can also be injected in any combination of the above, for example, into the throttle (102) and into the channel (103). The furnace reactor (100) includes multiple quenching positions (104a, 104b, 104c, 104d). The quenching medium is usually water, which reduces the temperature of the hot gas flow (or product mixture) and thus terminates the reaction that forms carbon black. Therefore, the position of the quenching has an impact on the residence time of the feedstock and the components derived from the feedstock. This means that if the quenching position is adjusted further downstream of the reactor, the residence time will increase. For example, quenching at position (104a) close to the throttle (102) will result in a shorter residence time, while quenching at position (104c) downstream of the reactor will result in a longer residence time. The reaction volume is the volume of the reactor between the feedstock injection point and the quenching position. If the feedstock is injected into the channel (103) with a distance of 4200 mm between the quenching position and the feedstock injection position and a channel diameter of 200 m, the resulting reaction volume is 132 L. The feed rate of the particulate carbonaceous feedstock should be adjusted according to the reaction volume mentioned in this specification. For the present invention, it is particularly preferred to arrange the quenching position at the rear of the channel to allow the particulate carbonaceous feedstock sufficient time to evaporate or pyrolyze.

[0298] refer to Figure 2 , shows a feeding and mixing device (200) comprising a carrier gas inlet (204), a particle inlet (201), a device for accelerating and injecting a carrier gas flow (207), a depolymerization duct (209), a mixing chamber (206) and an outlet (210) for the carrier gas entraining the particles. Figure 2The carrier gas channel (212) is also marked. The carrier gas channel (212) extends through the feeding and mixing device along the longitudinal axis. The carrier gas (203) enters the feeding and mixing device (200) through the carrier gas inlet (204) and is accelerated in the device for accelerating and injecting the carrier gas flow (207). Figure 2 In the embodiment, the device (207) for accelerating and injecting a carrier gas flow is configured as a Laval nozzle. The Laval nozzle includes a convergence zone (207a) in the flow direction. The generated carrier gas jet is injected into the mixing chamber (206). Particles such as the granular carbonaceous raw material (202) are injected vertically into the mixing chamber (206). Therefore, the particles will be entrained in the accelerated carrier gas. The sudden acceleration of the particles causes the particles to deagglomerate. The accelerated carrier gas containing the particles is further injected into the deagglomeration pipe (209). In the deagglomeration pipe (209), the particles collide with each other or with the inner wall or inner surface of the deagglomeration pipe (209), thereby achieving further deagglomeration. It is desirable that the device (207) for accelerating and injecting a carrier gas flow is configured so that the carrier gas jet is directly injected into the deagglomeration pipe (209). Therefore, the velocity loss can be minimized. The depolymerization pipe (209) generally includes an inlet funnel (209a) from downstream to upstream, a pipe (209b) with a constant inner diameter, and a diffusion nozzle (209c) diverging along the flow direction. The inlet funnel (209a) further enables entry into the pipe (209b) with a constant inner diameter with optimal flow behavior. The diffusion nozzle (209c) diverging along the flow direction also facilitates flow behavior. The outlet (406) can be connected to a Figure 1 A device for injecting raw materials into the reactor. Preferably, a feeding and mixing device (200) supplies the depolymerized raw materials to multiple devices for injecting raw materials into the reactor. It is further desired that the feeding and mixing device (200) includes a screw conveyor connected to the particle inlet (201). The screw conveyor can provide an appropriate amount or appropriate weight of particles into the mixing chamber (206). In addition, the feeding and mixing device (200) can be operated at a pressure of, for example, 1.5 bar or 2 bar. A pressure tank for particles (such as granular carbonaceous raw materials) can be installed. The pressure tank is fluidly connected to the particle inlet (201) and is preferably connected to the feeding and mixing device (200) by a valve. Preferably, there are two pressure tanks, wherein the first pressure tank is connected to the second pressure tank. The two pressure tanks can be connected by a valve.

[0299] Figure 3A Laval nozzle (300) for a feeding and mixing device (200) is shown. A carrier gas channel (306) extends through the Laval nozzle (300) along a longitudinal axis. A carrier gas (304) enters the Laval nozzle (300) and is accelerated. A carrier gas jet (305) then exits the Laval nozzle (300). The Laval nozzle (300) includes a portion (301) having a constant diameter, a portion (302a) converging along a flow direction (302), a throat (303a), and a diverging portion (303). In the Laval nozzle (300), the carrier gas is accelerated to a velocity greater than 1 Ma.

[0300] Furthermore, the present invention will be described through the following aspects.

[0301] Aspect 1. A feeding and mixing device for feeding particles into a reactor, comprising: (i) a carrier gas channel extending through the feeding and mixing device, (ii) at least one carrier gas inlet in fluid communication with the carrier gas channel, (iii) at least one particle inlet, (iv) a mixing chamber in fluid communication with the at least one particle inlet and the carrier gas inlet, (v) a deaggregation conduit in fluid communication with the mixing chamber, (vi) at least one outlet for the carrier gas to entrain the particles fed into the mixing chamber, wherein the at least one outlet is in fluid communication with the deaggregation conduit, and (vii) means for accelerating and injecting a flow of carrier gas into the mixing chamber.

[0302] Aspect 2. The feeding and mixing device according to aspect 1, wherein the gas channel extends through the feeding and mixing device along a longitudinal axis, and preferably the at least one inlet, the mixing chamber, the depolymerization duct and the outlet are aligned with the longitudinal axis.

[0303] Aspect 3. A feeding and mixing device according to any of the preceding aspects, wherein the particle inlet is configured to feed particles into the mixing chamber at an angle relative to the carrier gas jet discharged into the mixing chamber, preferably perpendicular to the carrier gas jet.

[0304] Aspect 4. The feeding and mixing device according to any of the preceding aspects, wherein the device for accelerating and injecting the carrier gas flow comprises at least one jet nozzle.

[0305] Aspect 5. The feeding and mixing device according to any of the preceding aspects, wherein the means for accelerating and injecting the carrier gas flow converges in a flow direction extending from the at least one carrier gas inlet toward the at least one outlet.

[0306] Aspect 6. The feeding and mixing device according to aspect 4 or 5, wherein the jet nozzle is a Laval nozzle.

[0307] Aspect 7. The feeding and mixing device according to any one of aspects 4 to 6, wherein the jet nozzle comprises a converging portion, a throat portion, and a diverging portion.

[0308] Aspect 8. A feeding and mixing device according to any one of Aspects 4 to 7, wherein the jet nozzle includes a diverging portion, and the angle of the diverging portion is 2° to 30°, preferably 3° to 20°, more preferably 4° to 15°, and most preferably 5° to 10°.

[0309] Aspect 9. A feeding and mixing device according to any one of Aspects 4 to 8, wherein the jet nozzle includes a converging portion, and the maximum inner diameter of the converging portion is 5 mm to 50 mm, preferably 8 mm to 40 mm, more preferably 10 mm to 30 mm, and most preferably 12 mm to 20 mm.

[0310] Aspect 10. A feeding and mixing device according to any one of Aspects 7 to 9, wherein the minimum inner diameter of the converging portion, the diverging portion and / or the inner diameter of the throat is 0.6 mm to 30 mm, preferably 1.2 mm to 18 mm, more preferably 1.9 mm to 12 mm, and most preferably 3 mm to 9 mm.

[0311] Aspect 11. The feeding and mixing device according to aspect 10, wherein the minimum inner diameters of the converging portion, the diverging portion, and the inner diameter of the throat are the same.

[0312] Aspect 12. A feeding and mixing device according to any one of Aspects 4 to 11, wherein the jet nozzle includes a diverging portion, and the maximum inner diameter of the diverging portion is 0.3 mm to 11 mm, preferably 0.5 mm to 7 mm, more preferably 0.9 mm to 5 mm, and most preferably 1.1 mm to 4 mm.

[0313] Aspect 13. A feeding and mixing device according to any one of Aspects 4 to 12, wherein the minimum inner diameter of the converging portion is greater than the maximum inner diameter of the converging portion, preferably the difference between the maximum inner diameters of the converging portion and the diverging portion is 5 mm to 30 mm, preferably 8 mm to 20 mm, more preferably 9 mm to 18 mm, and most preferably 10 mm to 15 mm.

[0314] Aspect 14. The feeding and mixing device according to any one of aspects 4 to 13, wherein the maximum inner diameter of the converging portion is greater than the maximum inner diameter of the diverging portion.

[0315] Aspect 15. A feeding and mixing device according to any one of Aspects 4 to 13, wherein the distance between the device for accelerating and injecting and the pipe with a constant inner diameter is 2 mm to 20 mm, preferably 2.5 mm to 15 mm, more preferably 3 mm to 10 mm, and most preferably 3.5 mm to 7 mm.

[0316] Aspect 16. The feeding and mixing device according to any of the preceding aspects, wherein the depolymerization conduit comprises a conduit having a constant inner diameter.

[0317] Aspect 17. The feeding and mixing device according to any of the preceding aspects, wherein the depolymerization pipeline comprises an inlet funnel from downstream to upstream, a pipeline with a constant inner diameter, and a diffusion nozzle diverging along the flow direction.

[0318] Aspect 18. The feeding and mixing device according to any of the preceding aspects, wherein the longitudinal axis of the depolymerization conduit is coaxial with the longitudinal axis of the feeding and mixing device.

[0319] Aspect 19. The feeding and mixing device according to any one of aspects 16 to 18, wherein the inner diameter of the pipe with a constant inner diameter is 1 mm to 20 mm, preferably 2 mm to 10 mm, more preferably 3 mm to 7 mm, and most preferably 4 mm to 6 mm.

[0320] Aspect 20. The feeding and mixing device according to any one of aspects 16 to 19, wherein the maximum inner diameter of the diffusion nozzle is larger than the inner diameter of the pipe having a constant inner diameter.

[0321] Aspect 21. A feeding and mixing device according to any one of aspects 17 to 20, wherein the maximum inner diameter of the diffusion nozzle is 5 mm to 50 mm, preferably 8 mm to 40 mm, more preferably 10 mm to 30 mm, and most preferably 12 mm to 20 mm.

[0322] Aspect 22. The feeding and mixing device according to any one of aspects 17 to 21, wherein the diverging nozzle and the converging portion of the jet nozzle have the same maximum inner diameter.

[0323] Aspect 23. A feeding and mixing device according to any one of aspects 16 to 22, wherein the angle of the diffusion nozzle is 1° to 30°, preferably 2° to 20°, more preferably 3° to 15°, and most preferably 4° to 8°.

[0324] Aspect 24. A feeding and mixing device according to any one of aspects 17 to 23, wherein the angle of the inlet funnel is 20° to 80°, preferably 30° to 75°, more preferably 40° to 70°, and most preferably 50° to 65°.

[0325] Aspect 25. A feeding and mixing device according to any one of aspects 17 to 20, wherein the maximum inner diameter of the diffusion nozzle is 5 mm to 50 mm, preferably 8 mm to 40 mm, more preferably 10 mm to 30 mm, and most preferably 12 mm to 20 mm.

[0326] Aspect 26. A feeding and mixing device according to any one of aspects 16 to 25, wherein the length of the pipe with constant inner diameter is 3 mm to 500 mm, preferably 5 mm to 200 mm, more preferably 10 mm to 50 mm, and most preferably 13 mm to 30 mm.

[0327] Aspect 27. A feeding and mixing device according to any one of aspects 16 to 26, wherein the length of the diffusion nozzle is 10 mm to 300 mm, preferably 20 mm to 200 mm, more preferably 25 mm to 150 mm, and most preferably 30 mm to 100 mm.

[0328] Aspect 28. The feeding and mixing device according to any one of aspects 16 to 27, wherein the inner diameter of the conduit having a constant inner diameter is larger than the maximum inner diameter of the outlet of the device for accelerating and injecting a flow of carrier gas.

[0329] Aspect 29. The feeding and mixing device according to any of the preceding aspects, wherein the means for accelerating and injecting the carrier gas flow, the mixing chamber and the depolymerization conduit are configured such that the carrier gas jet is discharged in the depolymerization conduit.

[0330] Aspect 30. The feeding and mixing device according to any of the preceding aspects, wherein the depolymerization conduit is configured as a diffuser.

[0331] Aspect 31. The feeding and mixing device according to any of the preceding aspects, further comprising at least one hopper located upstream of the at least one particle inlet.

[0332] Aspect 32. The feeding and mixing device according to any of the preceding aspects, further comprising at least one screw conveyor located upstream of the at least one particle inlet.

[0333] Aspect 33. The feeding and mixing apparatus according to any of the preceding aspects, wherein the particles are granular carbonaceous feedstock and the reactor is an entrained flow reactor for producing carbon black.

[0334] Aspect 34. The feeding and mixing device according to any of the preceding aspects, further comprising a pressure tank for the particles, wherein the pressure tank is in fluid communication with the at least one particle inlet and optionally with the at least one screw conveyor.

[0335] Aspect 35. A reactor system comprising a reactor and the feeding and mixing device according to any of the preceding aspects, wherein the feeding and mixing device according to any of the preceding aspects is in fluid communication with the reactor.

[0336] Aspect 36. The reactor system according to aspect 35, wherein the feeding and mixing device is connected to multiple inlets of the reactor, preferably through lances.

[0337] Aspect 37. A reactor system according to Aspect 35 or 36, wherein the reactor is an entrained flow reactor and the feeding and mixing device is connected to the restriction, combustion chamber and / or channel fluid upstream of the quenching zone of the entrained flow reactor.

[0338] Aspect 38. The reactor system according to any one of aspects 35 to 37, wherein the reactor is an entrained flow reactor, preferably a furnace reactor.

[0339] Aspect 39. A method for injecting granular material into a reactor, comprising the steps of: (a) deagglomerating the particles and entraining them in a carrier gas stream, preferably by using a feeding and mixing device according to any one of Aspects 1 to 34, and (b) injecting the carrier gas stream containing deagglomerated particles obtained in step (a) into the reactor.

[0340] Aspect 40. The method according to aspect 39, wherein the method is a method for producing carbon black, and the particulate material is a particulate carbonaceous feedstock, and the reactor is an entrained flow reactor for producing carbon black, preferably a furnace reactor.

[0341] Aspect 41. The method according to aspect 40, wherein the particulate carbonaceous feedstock is injected into the entrained flow reactor through multiple inlets, preferably through multiple lances.

[0342] Aspect 42. The method according to any one of aspects 39 to 41, wherein the carrier gas flow is accelerated and flows through the mixing chamber into the depolymerization channel.

[0343] Aspect 43. The method according to any one of aspects 39 to 42, wherein the deagglomeration is performed by accelerating the particles in a carrier gas stream and causing the particles to collide with the inner surface of the deagglomeration conduit.

[0344] Aspect 44. The method according to any one of aspects 39 to 43, wherein the carrier gas is accelerated to greater 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.

[0345] Aspect 45. The method according to any one of aspects 39 to 44, wherein the particles are affected by the carrier gas jet in a manner perpendicular to the carrier gas jet.

[0346] Aspect 46. The method according to any one of aspects 39 to 45, wherein the carrier gas stream containing the deagglomerated particles 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, and most preferably 0.8 bar to 1.2 bar.

[0347] Aspect 47. The method according to any one of aspects 39 to 46, wherein the carrier gas further comprises H2O and / or an additive.

[0348] Aspect 48. The method according to any one of aspects 39 to 46, wherein the carrier gas further comprises 1 to 10 vol% H2O.

[0349] Aspect 49. Use of the feeding and mixing device according to any one of aspects 1 to 34 for deagglomerating particulate, preferably particulate, carbonaceous feedstock.

[0350] Example

[0351] Example 1: Rubber particles

[0352] The experiment of Example 1 was carried out as follows Figure 1 The furnace reactor is shown in the small furnace reactor. The furnace reactor consists of a combustion chamber, a throttle, and a channel. The throttle reduces the diameter to 45 mm. A reactor channel with a diameter of 200 mm and a length of 4200 mm is installed downstream of the throttle.

[0353] Rubber particles are Figure 2 The feed and mixing device shown with a nozzle is injected into the furnace reactor within the throttling section. The reaction volume of the reactor is about 130 liters. The reaction volume is the reactor volume between the raw material injection point and the quenching point. The feed and mixing device depolymerizes the rubber particles by accelerating the granular carbon-containing raw materials. The rubber particles, i.e., the 0.0-0.5mm Gummigranulat (product number 005GUM) used in the experiment, were provided by ESTATO Umweltservice GmbH (ESTATO) in Germany. The rubber particles come from old tires and include synthetic rubber (SBR) and natural rubber (NR). The particle fraction is shown in Table 1. In addition, the weight average particle size (Dw50) is about 400μm, measured according to ASTM D 1511-12 (2017). However, different granular carbon-containing raw materials, such as plastic particles or biomass-based particles, can also be used.

[0354] Table 1: Particle size distribution of rubber particles from ESTATO measured according to ASTM D 1511-12 (2017).

[0355] Particle fraction <0.125mm 2.0 wt% Particle fraction 0.125–0.25 mm 9.6 wt% Particle fraction 0.25–0.50 mm 34.5% by weight Particle fraction 0.50–1.0 mm 45.1% by weight Particle fraction 1.0–2.0 mm 8.8 wt% Particle fraction <2.0mm 0.0 wt%

[0356] The properties of the rubber granules from ESTATO are shown in Table 2.

[0357] Table 2: Characteristics of rubber granules from ESTATO.

[0358]

[0359]

[0360] In addition, the rubber particles contain several metals, such as zinc and iron, at a mass fraction of about 300 ppm.

[0361] Determination of CHNS content by elemental analyzer

[0362] The carbon mass fraction, hydrogen mass fraction, nitrogen mass fraction and sulfur mass fraction are determined using an elemental analyzer with a thermal conductivity and infrared detector. This analyzer is a device for fully automatic quantitative analysis of the above elements. The combustion tube is heated to 1100°C and the reduction tube is heated to 850°C. A blank measurement is first performed. The carbon peak area value should be <50, the hydrogen peak area value should be <300, the nitrogen peak area value should be <50, and the sulfur peak area value should be <350. Otherwise, each adsorption column will be heated and then the blank measurement will be started again. The blank measurement value is calculated as follows:

[0363]

[0364] Where b is the blank measurement value, bi is the peak area of ​​each blank measurement value, n is the number of blank measurements, and i is an index from 1 to n.

[0365] The compensation for the blank measurement is calculated as follows,

[0366] acomp.=a–b,

[0367] where acomp. is the compensated peak area, a is the measured peak area, and b is the blank measurement value.

[0368] Next, the daily factor is measured. To do this, 3 mg of sulfonamide and 3 mg of a low-level standard (e.g., carbon black standard) are weighed into eight tin capsules. After weighing the respective samples, they are placed in a capsule press, covered with helium for 35 seconds, and then cold-sealed. Subtracting the blank value gives the relationship between the known theoretical element concentration of the standard sample and the actual calculated element concentration. The resulting daily factor must be between 0.9 and 1.1. If this is not the case, the measurements should be repeated using newly opened standards. Otherwise, a new calibration must be performed according to the manufacturer's instructions.

[0369] The daily factor is calculated as follows,

[0370]

[0371] Where f is the daily factor, c theor. is the theoretical factor, cact. is the actual calculated element concentration.

[0372] Then, eight tin capsules are weighed, each containing 5 mg ± 1 mg of the desired measured component, such as rubber particles. After weighing each sample, it is placed in a capsule press, blanketed with helium for 35 seconds, and then cold welded.

[0373] For measurement, the combustion tube is enriched with O2. The elements C, H, N and S burn to form CO2, H2O, NO x , SO2, and SO3. The halogens bound in the sample react to form volatile halogen compounds. In addition, WO3 particles are present in the combustion tube, acting as a catalyst to provide further O2, preventing the formation of non-volatile sulfates and binding interfering alkali and alkaline earth elements. The carrier gas stream is fed into a copper-filled reduction tube. In contact with the copper, nitrogen oxides (NOx) are completely reduced to N2. SO3 is reduced to SO2. Volatile halogen compounds are bound to silver wool.

[0374] N2 is not adsorbed and enters the thermal conductivity detector as the first measured component, while CO2, H2O and SO2 are adsorbed on their respective adsorption columns.

[0375] The adsorption columns are then heated one by one to the desorption temperature, allowing CO2 as a carrier gas to enter the thermal conductivity detector, followed by H2O, and SO2 to enter the infrared detector. The detectors emit digitized and integrated electrical signals based on the type and concentration of the component. The measurement signal is recorded as a function of time and displayed as an integrated value. The absolute elemental content of the sample is calculated using the integrated values ​​of each measured peak and calibration factors.

[0376] The element concentration is calculated according to the following equation,

[0377]

[0378] Where c is the element concentration (unit: %), a is the absolute content of the element (unit: mg), f is the daily factor, and w is the actual amount of the sample.

[0379] Determination of oxygen content by elemental analyzer

[0380] Based on the oxygen concentration, an electrical signal is transmitted from the elemental analyzer's thermal conductivity detector (WLD) to a microcontroller, which then displays it as an integrated value. By measuring the integrated value of the peak and combining it with a calibration factor, the absolute element content of the sample can be derived.

[0381] Heat the pyrolysis tube to 1050°C and perform a blank measurement first. The maximum oxygen peak area should be 200. If the blank value is not less than 200, heat the CO adsorption column (260°C, CO desorption 150°C). After successfully measuring the blank value, calculate the average blank area.

[0382] The blank measurement value is calculated as follows:

[0383]

[0384] Where b is the blank measurement value, bi is the peak area of ​​each blank measurement value, n is the number of blank measurements, and i is an index from 1 to n.

[0385] Next, the daily factor is measured. To do this, 3 mg of acetanilide is weighed into eight tin capsules. After weighing the corresponding sample, the capsule is placed in a capsule press, blanketed with helium for 35 seconds, and then cold-sealed. Subtracting the blank value yields the relationship between the known theoretical element concentration of the standard sample and the actual calculated element concentration. The resulting daily factor 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 performed according to the manufacturer's instructions.

[0386] The daily factor is calculated as follows,

[0387]

[0388] Where f is the daily factor, c theor. is the theoretical factor, c act. is the actual calculated element concentration.

[0389] Eight tin capsules are then weighed, each containing 5 mg ± 1 mg of the desired component, such as rubber particles. Each sample is weighed, placed in a capsule press, blanketed with helium for 35 seconds, and then cold welded. The sample is then measured.

[0390] The element concentration is calculated according to the following equation,

[0391]

[0392] Where c is the element concentration (unit: %), a is the absolute content of the element (unit: mg), f is the daily factor, and w is the actual amount of the sample.

[0393] Reaction conditions in furnace reactor

[0394] The reaction conditions for producing carbon black are shown in Table 3. The temperature of the hot gas stream after the feedstock injection was calculated as described in this specification. As mentioned above, the temperature (absolute temperature) can also be measured using a pyrometer. In addition, the residence time of particles with diameters of 0.5 mm and 1 mm was calculated. For this calculation, a pyrolysis modeling program was used.

[0395] Table 3: Reaction conditions in the furnace reactor.

[0396]

[0397] 1 273.15K and 101325Pa

[0398] 2 The k value is defined as the ratio of the stoichiometric amount of O2 required for complete stoichiometric combustion of the fuel to the amount of O2 supplied

[0399] Table 2: Continuation

[0400]

[0401]

[0402] After the rubber pellets were injected, the reaction was quenched with water, and the resulting carbon black was dried and ground to a volume-average particle size of approximately 5 μm. The carbon black obtained according to the present invention (see Experiments A1 to E12) was compared with standard carbon black N660 and recycled carbon black (rCB), which was recovered from the pyrolysis of rubber pellets.

[0403] The temperature inside the combustion chamber, i.e. the temperature of the hot combustion gases, is controlled by the temperature of the combustion air upstream of the combustion chamber (i.e. the temperature of the oxygen-containing gas). The k value is controlled by the flow rate of natural gas (fuel) entering the combustion chamber.

[0404] The carbon black produced comprises about 53 wt % recycled carbon black, about 27 wt % virgin carbon black and about 20 wt % ash. The recycled carbon black comprises coke. Since the rubber particles are used in the entrained flow reactor process, not only can the carbon black be recycled, but also virgin carbon black derived from the rubber can be produced. Therefore, the ash content is lower than that of recycled carbon black from REOIL (RCB615, about 23.2 wt % ash). The ash content can be measured according to ASTM D 1506-99 at 550° C. (16 hours).

[0405] The carbon black obtained in each experiment was characterized, and the results are shown in Table 4.

[0406] Table 4: Characterization of the obtained carbon black

[0407]

[0408]

[0409] 3 N550 carbon black, obtained from liquid feedstock, Orion Engineered Carbons GmbH.

[0410] 4 N660 carbon black, obtained from liquid feedstock, Orion Engineered Carbons GmbH.

[0411] 5 rCB2 recycled carbon black, REOIL SPZ OO.

[0412] 6 Aggregate size distribution is measured as follows.

[0413] 7 The specific surface area (AGV) is measured as follows.

[0414] 8 Volatiles, measured at 950°C for 7 minutes, are described below.

[0415] 9 BET surface area is measured according to ASTM D6556-21.

[0416] 10 STSA surface area is measured according to ASTM D6556-21.

[0417] 11 The iodine adsorption value is measured according to ASTM D1510-21.

[0418] 12 pH was measured according to ASTM D1512-21, Test Method B - Sonic Slurry.

[0419] 13 Compression Oil Absorption Number (COAN) is measured according to ASTM D3493-20 (using paraffin oil).

[0420] 14 Oil Absorption Number (OAN) is measured according to ASTM D2414-19 (using paraffin oil).

[0421] 15 The transmittance at 425 nm in toluene was measured using toluene according to ASTM D 1618-18 (transmittance of toluene extract).

[0422] Table 4: Continuation

[0423]

[0424]

[0425] Aggregate size distribution

[0426] All test results were analyzed according to ISO 15825:2016 using a Brookhaven BI-DCP disc centrifuge with a red light diode. The quoted test results are provided in the Brookhaven software after adjusting the appropriate parameters as described in the "Computer and Software Setup" section of ISO 185825:2017-03.

[0427] Specific surface area (AGV)

[0428] The specific surface area of ​​the test sample can be obtained in the Brookhaven software. After testing the sample and viewing the results, click "detailed" and read the "specific surface area (sq / g)" value on the computer screen.

[0429] Volatile matter at 950℃

[0430] The volatiles at 950°C were measured using a thermogravimeter (TGA-701) from Fa.LECO Instrumente GmbH according to the following protocol: the pan was dried at 650°C for 30 minutes. Before measurement, the carbon black material was stored in a desiccant equipped with a desiccant. The baked pan was placed in the instrument, tare, and loaded with 0.5g to 10g of carbon black material. The oven of the TGA instrument containing the sample pan was then gradually heated to 105°C by automatic software control, and the sample was dried until a constant mass was reached. Subsequently, the pan was covered, the oven was purged with nitrogen (99.9% by volume), and heated to 950°C. The oven temperature was maintained at 950°C for 7 minutes. The volatile content at 950°C was calculated using the following equation:

[0431]

[0432] result

[0433] Surprisingly it has been found that a particulate carbonaceous feedstock can be used in an entrained flow reactor process. As can be seen in Table 3, the carbon obtained has desirable properties compared to a standard carbon black product obtained from a liquid carbonaceous feedstock.

[0434] Furthermore, the agglomerate size and agglomerate surface area are smaller than those of recycled carbon black. This indicates that the resulting carbon black has a lower coke content. The specific surface area in the agglomerate size measurement further indicates the amount of coke present in the carbon black. Furthermore, large agglomerate size also indicates a high coke content.

[0435] Furthermore, as can be seen in Table 3, the residence time for A6 was 0.367 s, and the hot gas flow temperature was 1763°C. It is believed that the higher temperature resulted in an optimal residence time of 0.28 s for pellets with a diameter of 0.5 mm and 1.05 s for pellets with a diameter of 1 mm. The light transmittance of experiment B9, conducted using A6, was 95%. Light transmittance is an indicator of complete pyrolysis of the feedstock or C and H-containing compounds in the feedstock. Therefore, it is believed that higher temperatures and longer residence times are beneficial for producing carbon black from pelletized feedstock.

[0436] Example 2: Rubber composition

[0437] The preparation of the rubber compositions and rubber testing are described below.

[0438] The general production process of rubber compounds and their vulcanizates is described in the book “Rubber Technology Handbook”, W. Hofmann, Hanser Verlag 1994.

[0439] The rubber composition is shown in Table 5. ESBR Buna SB 1500 is placed in a laboratory mixer GK1.5E with a PES5 intermeshing rotor geometry manufactured by Harburg Freudenberger and ground for 30 seconds at a chamber temperature of 40°C, a fill factor of 0.66, and a rotor speed of 45 rpm. Subsequently, half the volume of carbon black, ZnO, and stearic acid is added under grinding conditions. After 90 seconds, the other half volume of carbon black and 6PPD is added. After another 90 seconds, the ram is lifted and cleaned, and the batch is then mixed for another 90 seconds. The total mixing time in the internal mixer is 5 minutes, after which the batch is poured into an open mill for cooling and additional distributive mixing. In the first mixing step, the batch temperature is no more than 160°C. The batch is allowed to stand overnight.

[0440] In the second and final mixing step, sulfur and an accelerator (Vulkacit CZ / EG-Z) were added to the masterbatch obtained in 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 rpm, ensuring that the batch temperature did not exceed 110°C. Finally, the mixture was removed from the internal mixer and processed again on an open mill. The resulting vulcanizable composition (green mix) was cured at 165°C for 11 to 15 minutes (C1: 15 minutes, C2: 12 minutes, C3: 12 minutes, C4: 12 minutes, C5: 11 minutes, C6: 12 minutes, C7: 12 minutes, C8: 11 minutes, and C9: 11 minutes).

[0441] Table 5: Rubber compositions using the different carbon blacks listed in Table 6.

[0442]

[0443] 16 Rubber ESBR, Buna SB 1500, Resinex Deutschland GmbH

[0444] 17 Carbon black: N660, N550, rCB or experiments A3 to A5 and A8 to A10 (see Table 6)

[0445] 18 6PPD, VULKANOX 4020 / LG, Brenntag GmbH

[0446] 19 Sulfur, MAHLSCHWEFEL 80 / 90° Avokal GmbH

[0447] 20 CBS, VULKACIT CZ / EG-C, Lanxess NV

[0448] 21 ZnO, ZNO RS RAL 844C, Norkem BV

[0449] 22 Stearic acid, Palmera B 1804, Caldic Deutschland GmbH

[0450] The properties of the samples were measured and the results are listed in Table 6. The results were compared with carbon blacks (N660 and N550) produced using liquid carbon black feedstock and recycled carbon black rCB.

[0451] Table 6: Properties of the produced carbon blacks in rubber compositions.

[0452]

[0453] 23 The loss factor tan(d) is measured as follows.

[0454] 24 The morphology relative peak area was measured as follows.

[0455] 25 Tensile strength was measured according to ISO 37-2012, S2.

[0456] 26 Elongation at break is measured according to ISO 37-2012, S2.

[0457] 27 Abrasion resistance was measured at 23° C. according to DIN ISO 4649:2014-03, 10 N.

[0458] 28 Modulus 300% is measured according to ISO 37-2012, S2.

[0459] 29 The coefficient of rebound is measured at 60°C according to ASTM D 2632:2015.

[0460] 30 The tear resistance is measured according to DIN ISO 34-1:2016-09, method B, variant (b).

[0461] experiment C5 C6 C7 C8 C9 carbon black A4 A5 A6 A7 A8 Loss factor tan(d) 0.153 0.155 0.159 0.154 0.152 Relative peak area of ​​morphology / % 4.43 3.59 6.13 2.7 3.2 Tensile strength / Mpa 25.4 25 25.2 25.6 26.6 Elongation at break / % 629 655 651 612 665 <![CDATA[Wear resistance (Abrasion) / mm 3 > 105 114 112 107 117 Modulus 300% / Mpa 6.1 5.8 5.9 6.9 5.6 Ballrebound 62.2 62.4 61.6 61.7 62.8 <![CDATA[Tear resistance GRAVES 30 > 19.1 19.7 19.1 20.2 18.4

[0462] Morphology relative peak area

[0463] The topographic relative peak area is an indicator of the filler dispersion determined by surface topography measurements 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 19917975 C2 (including Medalia correction).

[0464] Loss factor tan(d)

[0465] The above values ​​and the loss factor tan(d) are measured in accordance with DIN 53513 in strain-controlled mode (1±0.5 mm) or force-controlled mode (50 N±25 N) on cylindrical test pieces (height 10 mm, diameter 10 mm) at 60° C. and a frequency of 16 Hz.

[0466] result

[0467] The examples show that the carbon blacks produced according to the invention (Carbon Blacks A3-A5, A8-A10) can be advantageously used in rubber compositions (Experiments C5 to C10). The carbon blacks produced have a low loss factor tan(d), high topography, and high tensile strength. Furthermore, the elongation at break is preferably between 612% and 665%. The rebound resilience of the carbon blacks produced is comparable to that of Carbon Black N660 and Carbon Black N550.

[0468] It will be understood that various modifications can be made and that many changes can be made to the preferred embodiments without departing from the principles of the invention.

Claims

1. A feeding and mixing device for feeding particles into a reactor, comprising: (i) a carrier gas passage extending through the feeding and mixing device, (ii) at least one carrier gas inlet in fluid communication with the carrier gas channel, (iii) at least one particle inlet, (iv) a mixing chamber in fluid communication with the at least one particle inlet and the carrier gas inlet, (v) a deagglomeration conduit in fluid communication with the mixing chamber, (vi) at least one outlet for a carrier gas entrained with particles fed to the mixing chamber, wherein the at least one outlet is in fluid communication with the depolymerization conduit, and (vii) means for accelerating and injecting a stream of carrier gas into said mixing chamber.

2. A feeding and mixing device according to claim 1, wherein the particle inlet is configured to feed particles into the mixing chamber at an angle relative to the carrier gas jet discharged into the mixing chamber, preferably perpendicular to the carrier gas jet.

3. The feeding and mixing device according to claim 1 or 2, wherein Said means for accelerating and injecting the carrier gas flow comprise at least one jet nozzle, preferably a Laval nozzle.

4. The feeding and mixing device according to any one of the preceding claims, wherein the depolymerization conduit comprises an inlet funnel from downstream to upstream, a conduit with a constant inner diameter and a diffusion nozzle diverging in the flow direction.

5. The feeding and mixing device according to any one of the preceding claims, further comprising at least one screw conveyor located upstream of the at least one particle inlet.

6. A feeding and mixing device according to any one of the preceding claims, wherein the particles are a carbonaceous feedstock and the reactor is an entrained flow reactor for the production of carbon black.

7. A reactor system comprising a reactor and a feeding and mixing device according to any one of the preceding claims, wherein the feeding and mixing device is in fluid communication with the reactor.

8. Reactor system according to claim 7, wherein the feeding and mixing means are connected to a plurality of inlets of the reactor, preferably via lances.

9. The reactor system according to claim 7 or 8, wherein the reactor is an entrained flow reactor, preferably a furnace reactor.

10. A method of injecting granular material into a reactor, the method comprising the steps of: (a) deagglomerating the particles and entraining them in a carrier gas stream, preferably by using a feeding and mixing device according to any one of claims 1 to 6, (b) injecting the carrier gas stream containing the deagglomerated particles obtained in step (a) into the reactor.

11. The method according to claim 10, wherein the method is a method for producing carbon black, and the particles are granular carbonaceous feedstock, and the reactor is an entrained flow reactor for producing carbon black, preferably a furnace reactor.

12. The method according to claim 11, wherein the particulate carbonaceous feedstock is injected into the entrained flow reactor through a plurality of inlets, preferably through a plurality of lances.

13. The method according to any one of claims 10 to 12, wherein the carrier gas flow is accelerated and flows through a mixing chamber into a depolymerization conduit, and / or wherein the carrier gas is accelerated to a velocity greater 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.

14. The method according to any one of claims 10 to 13, wherein the carrier gas further comprises H2O and / or additives, preferably the carrier gas further comprises H2O in an amount of 1% to 10% by volume.

15. Use of the feeding and mixing device according to any one of claims 1 to 6 for deagglomerating particles, preferably particulate carbonaceous feedstock.

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