KR930005684B1 - Method for controlling the aggregate size and structure of carbon blacks - Google Patents

Abstract

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Description

How to control the size and structure of carbon black aggregates

1 is a cross sectional view of one embodiment of the present invention showing first and second quenchs in a carbon black reactor.

* Explanation of symbols for main parts of the drawings

10 reactor 12 reaction zone

14,60,62: point 20: limited diameter band

30: raw material 40: first cooler

42: second cooler 50: coolant

The present invention relates to a method for controlling the size and structure of carbon black aggregates.

Carbon black is generally obtained by pyrolysing a hydrocarbon feedstock with a hot combustion gas in a reactor in the form of a furnace to produce combustion products containing particulate carbon black.

Fuel is preferred in the furnace-type carbon black reactor (hereinafter abbreviated as "Kester" and "Flock") as disclosed in U.S. Patent No. 3,401,020 to Kester et al. Or US Pat. No. 2,785,964 to Plocklock et al. In the following, a hydrocarbon fuel and an oxidant, preferably air, are injected into the first zone to react to form a hot combustion gas. Hydrocarbon feedstock, taking either gaseous, vapor or liquid form, is also injected into the first zone, where pyrolysis of the hydrocarbon feedstock occurs. In this case, pyrolysis means pyrolysis of hydrocarbons. The resulting combustion gas mixture with pyrolysis taking place then enters the reaction zone where the carbon black formation reaction is completed.

In another form of carbon black reactor, liquid or gaseous fuel is reacted with an oxidant, preferably air, in the first zone to form a hot combustion gas. This hot combustion gas flows from the first zone through the reactor in the downstream direction of the reaction zone and below. Hydrocarbon feed is injected into the passage of a hot combustion gas stream at one or more points to produce carbon black. The hydrocarbon feedstock is liquid, gas or steam and may be the same as or different from each other with the fuel used to form the combustion gas stream. The first (or combustion) zone and the reaction zone may be separated by chokes or zones having a limited diameter whose cross section is smaller than the combustion zone or reaction zone. The raw material may be injected upstream, downstream and / or in the passage of the hot combustion gas stream in the zone having a limited diameter. Low carbon black reactors of this type are generally described in US Pat. No. 28,974 and US Pat. No. 3,922,335. Although two types of furnace carbon black reactors and processes have been described, it should be understood that the present invention can be used in any other furnace carbon black reactors or processes where carbon black is produced by pyrolysis and / or incomplete combustion of hydrocarbons.

In the two types of processes and reactors described above, and other generally known reactors and processes, the hot combustion gases have a temperature sufficient to pyrolyze the hydrocarbon feed injected in the combustion gas strip. In one reactor form as disclosed in the Caster patent, the raw material is injected in the same zone where the combustion gases are formed at one or more points. In other types of reactors and processes, raw material injection occurs at one or more points after the combustion gas stream is formed. In all types of reactors, the hot combustion gas stream flows continuously through the reactor in the downstream direction so that continuous pyrolysis occurs as it passes through the reaction zone of the mixture of raw material and combustion gas. The mixture of raw materials and combustion gases in which pyrolysis takes place is referred to herein as "effluent" throughout the specification. The time for which the effluent remains in the reaction zone of the reactor is sufficient to form carbon black under suitable conditions. "Reaidence time" means the amount of time that has elapsed since the first contact of the hot combustion gas with the raw material. After the carbon black having the predetermined characteristics is formed, the temperature of the effluent is further lowered to stop pyrolysis. This lowering of the temperature of the effluent to stop the pyrolysis can be achieved by known methods, for example by spraying the coolant to the effluent via a quench. As is generally known to those skilled in the art, pyrolysis is stopped when certain carbon black products are produced in the reactor. One way to determine when pyrolysis should be stopped is by sampling the effluent and measuring its toluene extraction concentration. Toluene extraction concentration is measured according to ASTM D1618-83 "Carbon Black Extractable-Toluene Discoloration". The cooler is generally located at a point where the toluene extraction concentration of the effluent reaches a level that allows the desired carbon black product to be produced in the reaction. After the pyrolysis is stopped, the effluent is usually separated and collected by passing through a bag filter system.

Generally one cooler is used. However, the caster patent discloses the use of two coolers to control certain properties of carbon black. The caster patent relates to a method of controlling the modulus imparting properties of carbon black by heat treatment. This heat treatment is accomplished by controlling the flow rate of water with two water jet coolers arranged in series in the effluent steam to carbon black. The modulus of carbon black is related to the performance of carbon black in rubber products. Schaefer and Smith's paper "The Effect of Heat Treatment on the Reinforcement of Carbon Black" (Industrial and Engineering Chemistry, Vol. 47, No.6; June 1955, page 1286) (hereinafter abbreviated as "Schaefer") In general, heat treatment is known to affect the modulus imparting properties of carbon black. However, as further described in Schaefer's paper, the change in modulus imparting properties of carbon black resulting from heat treatment results in a surface chemical change of carbon black. Thus, placing the cooler as suggested by Caster to place the combustion gas stream under different temperature conditions, the modulus imparting properties of carbon black obviously affect the morphology of carbon black in some unrecognizable manner. It is affected by changing the surface chemistry of carbon black rather than by giving it. Furthermore, in the caster patent two coolers were placed in a position in the reaction zone where the pyrolysis of the raw material had already advanced considerably. Therefore, the caster method is expected to define the physical properties of carbon black, such as CTAB, color tone, DBP and Stokes diameter, with the time that the effluent reaches the first cooler. This supports the conclusion that the change in modulus imparting properties in the caster method is not due to the change in morphology properties of carbon black. In addition, the caster did not attach any importance to the position of the first cooler relative to the injection time or the residence time of the raw material, and did not describe a method of selecting the position of the first cooler.

Forseth, US Pat. No. 4,230,670 (hereinafter abbreviated as " Forceset ") has proposed a method for stopping pyrolysis using two coolers. The two coolers are located several inches away from the point where one cooler will be located. The purpose of the two coolers is to more effectively stop the pyrolysis by more fully filling the reaction zone with the coolant. Such a Porsset method defined the CTAB, color tone, DBP and Stokes diameter characteristics of Keybone Black with the time that the effluent reached the two coolers.

US Pat. Nos. 4,265,870 and 4,316,876 to Mills et al. Proposed the use of a second cooler downstream of the first cooler to prevent damage to the filtration device. In both patents, the first cooler is located at a location generally known in the art to completely stop pyrolysis, and the CTAB, tint, DBP and Stokes diameter of carbon black is the time that the effluent reaches the first cooler. The characteristics were limited. The second cooler further lowers the temperature of the combustion gas stream to protect the filtering device.

Austin, US Pat. No. 4,358,289 (abbreviated herein as “Austin”) also relates to a method of preventing damage to the filtration device by using a heat exchanger after the cooler. In this patent too, the cooler completely stops pyrolysis and is located in a position generally known in the art. The Austin patent defined the CTAB, color tone, DBP and Stokes diameter characteristics of carbon black by the time the effluent reached the first cooler.

Lewis, US Pat. No. 3,615,211 (hereinafter abbreviated as "Lewis") relates to a method of improving the uniformity of carbon black produced in the reactor and to extending the life of the reactor. Lewis suggested using a plurality of coolers located throughout the reaction zone to substantially maintain the temperature of the reaction zone to improve uniformity and extend reactor life. A certain amount of coolant is sprayed in the cooler located most upstream of the reactor, and a larger amount of coolant is each continued in the cooler downstream. The downstream cooler stops pyrolysis. By keeping the temperature constant in the reaction zone, Lewis's device enhanced the uniformity of the carbon blacks made with this device. However, many coolers did not control the morphology of Gabon Black made with this device.

However, it is generally desirable for the morphology of the carbon black to be adjustable so that the carbon black can be made to be well suited for a particular end use. It is also desirable to increase the aggregate size and structure of carbon black for a given surface area. The reason is that the increased aggregate size and structure makes the carbon black more suitable for a particular end use, as indicated by higher DBP, lower tint and larger Stokes number diameter.

Accordingly, it is an object of the present invention to provide a method of controlling the aggregate size and structure of carbon black.

Another object of the present invention is to produce carbon blacks having a larger aggregate size and structure at a given surface area.

The inventors have found a way to achieve these desirable objects. The inventors have found that the morphology of the carbon black produced in the low carbon black process maximizes the temperature of the effluent without stopping pyrolysis, preferably within a specified retention time of up to about 0.002 in the downstream direction at the most downstream raw material injection point. It was found that it could be controlled by lowering to an amount of about 426.7 ° C (800 ° F). The temperature reduction can be achieved by placing the first cooler about 4 feet downstream or within about 4 feet downstream of the most downstream point of the raw material injection point and the coolant injection point. According to the present invention, the production of carbon black has specific morphological properties such as higher DBP, lower color tone and larger aggregate size and increased structure, represented by increased Stokes diameter (CTAB) for a given surface area. It can be adjusted to produce carbon black. The inventors have also found that these morphological properties of carbon black can be controlled by changing the temperature drop of the effluent and / or by changing the residence time from the raw material injection time on the most downstream until the temperature of the effluent drops. .

More specifically, the present invention relates to aggregate materials and structures of the carbon blacks produced in the raw carbon black reactor, not by stopping the pyrolysis occurring in the effluent (a mixture of the combustion gas and the raw material in which the pyrolysis takes place), And a method of controlling by lowering the temperature of the effluent within a residence time between about 0.0 seconds and 0.002 seconds, preferably between about 0.0 seconds and 0.0015 seconds, downstream from the injection point. The temperature of the effluent falls within this particular residence time, preferably in an amount up to about 426.7 ° C., more preferably from about 10 ° C. to 426.7 ° C. The temperature of the effluent is about 0.0 to 0.002 seconds, preferably about 0.0, downstream from the raw material injection point of the downstream by spraying the coolant to the effluent with a cooler, preferably a cooler located at a point in the reactor. It falls by cooling within 0.0015 second. Typically, to cool the effluent within a certain residence time, the chiller will have to be located at or within about four feet of the most downstream raw material injection point. The cooler lowers the temperature of the effluent to preferably up to about 426.7 ° C., more preferably from about 10 ° C. to 426.7 ° C., without stopping pyrolysis. According to the present invention, the size and structure of the aggregates of the carbon black produced in the reactor can be controlled by changing the amount of temperature decrease of the effluent and the residual temperature at which the temperature of the effluent occurs independently or simultaneously. In a reaction using a cooler that injects a coolant for lowering the temperature of the effluent within a certain residence time, the change in the amount of temperature decrease of this effluent and the residence time at which the temperature decrease of the effluent occurs is caused by the amount of coolant injected from the cooler and the cooler. This can be accomplished by varying the position of. After the carbon black having the predetermined characteristics is formed, the pyrolysis is stopped.

According to the invention, it is possible to obtain carbon black products having a larger aggregate size and structure for a given surface area than carbon black produced by other similar methods in which the temperature of the effluent does not fall within a certain residence time.

The method of the present invention has the advantage of being able to control the aggregate size and structure of the carbon black.

Another advantage of the process of the present invention is that it is possible to produce carbon blacks with larger DBPs, larger aggregate sizes and structures represented by lower hue, and increased Stokes diameters represented by CTAB for a given surface area.

Still other advantages of the present invention will become apparent from the following description and claims.

The drawings illustrate one possible embodiment of the present invention. Although a portion of one type of carbon black reactor is shown in the figures, the present invention can be used in the reactor with any carbon black that produces carbon black by pyrolysis and / or incomplete combustion of hydrocarbons. In addition, the following description describes one embodiment of the present invention using a cooler to inject a coolant to lower the temperature of the effluent, but as will be appreciated by those skilled in the art, the present invention is directed to the temperature of the effluent, Preferred amounts include all methods of lowering in a predetermined amount of time within a set residence time from the raw material injection point nearest the reaction zone. Likewise, the following description describes a second cooler used to stop pyrolysis, but as will be appreciated by those skilled in the art, the present invention includes all methods of stopping pyrolysis.

In the figure, for example, a first cooler 40 and a second cooler 42 for injecting a coolant 50 into a portion of the carbon black reactor 10 having a reaction zone 12 and a limited diameter zone 20. ) Were installed at points 60 and 62, respectively. The coolant 50 may be the same or different from each other in each cooler. The direction in which the hot combustion gas stream flows through reactor 10 and zones 12 and 20 is shown by arrows. The coolant 50 may be injected into the first cooler 40 and the second cooler 42 in the reverse direction to the direction of the combustion gas stream, or preferably in the same direction. Point 14 is the most downstream raw material injection point. As will be appreciated by those skilled in the art, the most downstream raw material injection point 14 can be varied. The distance from the most downstream raw material injection point 14 to the position point 60 of a 1st cooler is represented by L-1, and is located from the most downstream raw material injection point 14 to the position point 62 of a 2nd cooler. The distance of is represented by L-2.

According to the illustrated embodiment of the present invention, the first cooler 60 has a effluent (combustion gas with pyrolysis occurring within 0.002 seconds, preferably 0.0-0.0015 seconds, which is a residence time from the most downstream raw material injection point. And a mixture of raw materials). Typically, the first cooler is positioned at or within about 4 feet of the most downstream raw material injection point to cool the effluent within the designated residence time. Thus, L-1 will be about 0.0-4 feet. The coolant is sprayed through the first cooler to lower the temperature of the effluent to an amount of preferably up to about 426.7 ° C., more preferably about 10 ° C.-426.7 ° C. However, the cooling liquid injected through the first cooler 60 does not stop the pyrolysis.

Further, according to the present invention, the temperature of the effluent (a mixture of the combustion gas and the raw material in which pyrolysis takes place) from the downstream raw material injection point is independently or simultaneously with the amount of the residence time and the amount of the temperature of the effluent decreasing until the first decrease. By changing, the size and structure of the aggregates of carbon black produced in the reactor can be controlled. In the embodiment of the present invention shown in the accompanying drawings, changing L-1 will change the residence time from the most downstream raw material injection time to the time when the temperature of the effluent falls. By changing the injection amount of the cooling liquid, it is also possible to change the temperature lowering amount of the effluent.

As described above, in the embodiments of the present invention shown in the figures, the desired aggregate size and structure typically depends on the L-1 range of about 0.0-4 feet. Cooling liquid 50 lowers the temperature of the effluent, preferably up to about 426.7 ° C, more preferably about 10-426.7 ° C. However, pyrolysis is not stopped by the cooling liquid 50 in the first cooler 60.

After the carbon black having the desired properties is produced, the pyrolysis is stopped at the point 62 by the cooler 42. Point 62 is where carbon black with the desired properties is produced by the reactor. As described above, point 62 may be determined by methods known in the art as a method of selecting the installation location of the cooler to stop pyrolysis. One method of determining the installation location of the cooler to stop pyrolysis is to determine the installation point by measuring the point at which an acceptable toluene extraction concentration is obtained for a given carbon black product obtained from the reactor. Toluene extraction concentration can be measured using ASTM Test D 1618-83 "Carbon Black Extractables-Toluene Discoloration". L-2 will vary depending on the location of point 62.

The effects and advantages of the present invention will be described in more detail in the following non-limiting examples.

EXAMPLE

In order to prove the effect of the present invention, the present invention is used in a carbon black manufacturing process that uses two coolers and changes the residence time from the raw material injection time on the downstream side until the temperature of the effluent is lowered and the amount of the temperature of the effluent is lowered. An experiment was performed on. The residence time was changed by changing L-1. Process parameters and results for the two sets of carbon blacks used in the experiments are summarized in the table below. Set I consisted of run numbers 1, 2 and 3, and set II comprised run numbers 4, 5 and 6.

Set I: Preheat = 482.2 ° C. (900 ° F.), Gas = 7.2 Kscfh, Air = 80 Kscfh, Air / Gas = 11.11, Primary Combustion Rate = 123%, Combustion Zone Volume = 85ft ³ , Injection Zone Diameter = 4.2 Inch Injection Zone Length = 12 inches, combustion gas velocity in injection zone = 2000 ft / sec, oil = 125 gph, oil injection pressure = 230 psig, number of oil tips = 4, oil tip diameter = 0.042 inches, reaction zone diameter = 13.5 inches, The composition of the raw material liquid (oil) is as follows. H / C ratio = 0.91; Hydrogen = 6.89 wt%, 7.00 wt%; Carbon = 99.1 wt%, 90.8 wt%, Sulfur = 1.1 wt%, API specific gravity 15.6 / 15.6 ° C. (60 ° F.) =-5.0, BMCI (viscosity-weight) = 141

Set II: Preheating = 1100 ° F, Gas = 7.5Kscfh, Air = 80Kscfh, Air / Gas = 10.6, Primary Combustion Rate = 118%, Combustion Zone Volume = 0.85ft ³ , Injection Zone Diameter = 4.2inch, Injection Zone Length = 12 Inch, combustion gas velocity in injection zone = 2300 ft / arc, oil = 136 gph, oil injection pressure = 270 psig, number of oil tips = 4, oil tip diameter = 0.042 inches, reaction zone diameter = 6 inches, stock solution The composition of (oil) is as follows. H / C ratio = 1.06; Hydrogen = 7.99 wt%, 7.99 wt%; Carbon = 89.7 wt%, 89.5 wt%, Sulfur = 0.5 wt%, API specific gravity 15.6 / 15.6 ° C. (60 ° F.) = 5.0, BMCI (viscosity-weight) = 123.

The liquid fuel used during the combustion reaction in both Set I and Set II is natural gas with a methane content of 95.44% and a wet calorific value of 925 BTU / SCF.

As will be appreciated by those skilled in the art, the process variables described in the table mean the variables at one point in the reactor and are determined by known methods. Each set of carbon black samples was prepared in a carbon black reactor similar to the reactor described in Example 1 of US Pat. No. 3,922,335, except as noted in the table.

In the table, Q means cooler, and 1stQ ft. Means distance L-1 from the raw material injection point on the most downstream side to the first cooler. The temperature before the first cooler (Temp.Bef.1stQ) refers to the temperature of the effluent before the first cooler, the temperature after the first cooler (Temp.Aft.1stQ) and the temperature after the second cooler (Temp.Aft). .2ndQ) means the temperature of the effluent after the first cooler and the temperature of the mixture of raw material and combustion gas after the second cooler, respectively. All temperatures involved in cooling were calculated by conventionally known thermodynamic methods. Res.Time in the table means the amount of time that has passed since the downstream injection of the raw material, ie the time that elapsed before the effluent temperature first lowered. 2ndQ ft. Means L-2 and was determined empirically using toluene extraction concentration. After performing each set, the produced carbon black was recovered and analyzed by CTAB, color tone, Dst (average Stokes diameter), CDBP, baffle DBP and toluene discoloration. The gks results for each run are shown in the table.

CTAB was measured according to ASTM Test Procedure D 3765-85. Tint was measured according to ASTM Test Procedure D 3265-85q. DBP of baffle black was measured according to the method described in ASTM D-2414-86. CDBP was measured according to the method described in ASTM D 3493-86. Toluene discoloration was measured according to ASTM Test Procedure D 1618-83.

Dst (Average Stroke Diameter) was measured by disc centrifuge photosedimentometry according to the description below. The instructions are as follows: Instruction Manual for thd Joyce-Loebl Disc, purchased from Joyce-Loebl Company, Dean & Ware Gateshed Tim Valley Marquisway, UK. Centrifuge, file reference number DC F4.008, published February 1, 1985) is a modification of the method. This document is incorporated herein by reference. This method is as follows. After weighing 10 mg of carbon black sample in a weighing vessel, 0.05% NONIDET P-40 surfactant with 10% anhydrous ethanol and 90% distilled water (this NONIDET P-40 is manufactured and sold by Shell Chemical Co., Ltd.). Was added to 50 cc of the prepared solution. This suspension is manufactured and sold by Heat Systems Ultrasonics Inc. of Farmingdale, New York. W385 was used to disperse ultrasonic energy for 15 minutes. Prior to operating the disc centrifuge, the following data was entered into a computer recording data from the disc centrifuge.

1. Specific gravity of carbon black; 1.86 g / cc

2. volume of carbon black solution dispersed in water and ethanol solution; In this case 0.5 cc,

3. the volume of the rotating fluid; In this case 10 cc of water,

4. viscosity of rotating fluid; In this case, 0.933 centipoise at 23 ° C,

5. Density of rotating fluid; In this case 0.9975 g / cc at 23 ° C.,

6. disk speed; In this case 8000 rpm,

7. sampling time interval of data; 1 second in this case.

The disc centrifuge was operated at 8000 rpm while operating the strobosk. 10 cc of distilled water was sprayed on the rotating disk as a rotating liquid. The cloudiness level was fixed at 0, and 1 cc of a solution of 10% dry ethanol and 90% distilled water was injected as a buffer. The blocking and acceleration buttons of the disc centrifuge were operated to obtain a lubricated concentration gradient between the rotating fluid and the buffer. If the gradient was lubricated such that no noticeable boundary was seen between the two emulsions, 0.5 cc of carbon black dispersed in ethanol solution was sprayed into the spinning disk and data were immediately collected. If a stream occurs, the operation has failed. The disk centrifuge was rotated for 20 minutes followed by spraying carbon black dispersed in aqueous ethanol solution. After rotating for 20 minutes, the disk centrifuge was stopped, the temperature of the rotating liquid was measured, and the average temperature of the rotating liquid measured at the beginning of the operation and the temperature of the rotating liquid measured at the end of the operation were recorded from the disk centrifuge. It was entered into the recording computer. The data were analyzed according to standard Stokes equations and presented using the following definitions.

Carbon black aggregate-isolated hard colloidal entity that is the smallest dispersible unit. It is composed of widely coalesced particles.

Stokes Diameter-The diameter of a globular body that settles in a viscous medium in a centrifugal or gravitational field according to the Stokes equation. Non-spherical objects, such as carbon black aggregates, can be represented by Stokes diameter if they can be considered to behave like smooth, hard spheres with the same density and sedimentation rate as this object. Typical units are expressed in nm diameter.

Average Stokes Diameter (Dst for Reporting Purposes) —Point on the distribution curve of Stokes Diameter when 50% by weight of the total sample is greater or smaller. Therefore, this is the average value of the measured values.

As shown in the table, the present invention provides an increased CDBP, baffle DBP and Dst and carbon with reduced color tone compared to the carbon black produced by Comparative Carbon Black Manufacturing Process Run Nos. 1 and 4 using one cooler. It allows the manufacture of black. This fact shows that the carbon black of the present invention is characterized by increased aggregate size and structure. Furthermore, as shown as a result for Set II, the present invention allows the production of carbon black with increased CDBP, baffle DBP and Dst and reduced color tone for relatively constant CTAB. This fact shows that the present invention produces carbon blacks with increased aggregate size and structure for a given CTAB.

As shown as a result for set I, the present invention provides increased CDBP, baffle DBP and Dst compared to carbon black obtained by comparative carbon black manufacturing process run number 1 at different residence times for which the temperature of the effluent was initially lowered by the same amount. And carbon black having reduced color tone.

Since the present invention relates to a method for controlling the aggregate size and structure of the carbon black, various modifications and modifications can be made according to the above-described carbon black production examples without clearly changing the gist of the present invention. Accordingly, the invention described in the specification and shown in the accompanying drawings is merely illustrative and is not intended to limit the scope of the invention. The invention includes all modifications falling within the scope of the following claims.

Claims (20)

pyrolysis of the raw material is initiated in this effluent by (a) passing a hot combustion gas stream through the reactor and (b) injecting the raw material into the hot combustion gas stream at one or more points to form an effluent. (c) at the first point within 0.002 seconds of the downstream direction from the injection point of the downstream material, the aggregates of carbon black and the structure of reducing the temperature of the effluent without stopping the thermal decomposition of the material occurring in the effluent. How to adjust. The method of claim 1, wherein the temperature drop of the effluent is at most about 426.7 ° C. (800 ° F.). The method of claim 1, wherein the temperature drop of the effluent is between 10 ° C and 426.7 ° C. The method of claim 1 wherein the temperature drop of the effluent occurs within a time of 0.0 seconds to 0.0015 seconds from the most downstream raw material injection point. 4. A method according to claim 3, wherein the temperature drop of the effluent occurs within a time of 0.0 seconds to 0.0015 seconds from the most downstream raw material injection point. A method according to claim 1, wherein the temperature drop of the effluent is caused by the injection of the cooling liquid. 7. The method of claim 6, wherein the temperature drop of the effluent occurs within a time of 0.0 seconds to 0.0015 seconds from the most downstream raw material injection point. 7. The method of claim 6, wherein the amount of temperature decrease of the effluent by the cooling liquid is at most about 426.7 ° C. 7. A method according to claim 6, wherein the temperature drop of the effluent by the coolant is between 10 ° C and 426.7 ° C. 8. The method of claim 7, wherein the amount of temperature decrease of the effluent by the coolant is between 10 ° C and 426.7 ° C. pyrolysis of the raw material is initiated in this effluent by (a) passing a hot combustion gas stream through the reactor and (b) injecting the raw material into the hot combustion gas stream at one or more points to form an effluent. (c) at the first point in the direction of 0.002 seconds downstream from the most downstream raw material injection point, the temperature of the effluent is lowered without stopping the thermal decomposition of the raw materials occurring in the effluent, and (d) being downstream of the first point. Further lowering the temperature of the effluent at the second point to stop pyrolysis of the raw materials occurring in the effluent, and (e) to separate and collect the carbon black product. The method of claim 11, wherein the temperature drop of the effluent is at most about 426.7 ° C. (800 ° F.). 12. The method of claim 11, wherein the temperature drop of the effluent is between 10 ° C and 426.7 ° C. 12. The method of claim 11, wherein the temperature drop of the effluent occurs within a time of 0.0 seconds to 0.0015 seconds from the most downstream raw material injection point. 15. The method of claim 13, wherein the temperature drop of the effluent occurs within a time of 0.0 seconds to 0.0015 seconds from the most downstream raw material injection point. 12. The method of claim 11, wherein the temperature drop of the effluent is caused by injection of the cooling liquid. 17. The method of claim 16, wherein the temperature drop of the effluent occurs within a time of 0.0 seconds to 0.0015 seconds from the most downstream raw material injection point. The method of claim 16, wherein the amount of temperature decrease of the effluent by the cooling liquid is at most about 426.7 ° C. 18. 17. The method of claim 16, wherein the amount of temperature decrease of the effluent by the coolant is between 10 ° C and 426.7 ° C. 18. The method of claim 17, wherein the amount of temperature decrease of the effluent by the coolant is between 10 ° C and 426.7 ° C.

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