JPH0749541B2 - Carbon black manufacturing method - Google Patents

Description

TECHNICAL FIELD OF THE INVENTION The present invention relates to a method for controlling the size and structure of aggregates of carbon black.

[Conventional method]

Carbon black is generally produced in a furnace reactor by pyrolyzing a hydrocarbon feedstock with a hot combustion gas to produce a combustion product containing particulate carbon black.

US Pat. No. 3,401,020 to Kester et al. Or US Pat. No. 2,785,964 to Pollock (hereinafter
In one type of furnace carbon black reactor, referred to as "Kester" and "Pollock" respectively, a fuel, preferably a hydrocarbonaceous fuel, and an oxidant, preferably air, are It is injected into the zone and reacts to produce hot combustion gases. Also, either the gaseous, vaporous or liquid form of the hydrocarbon feedstock is injected into the first zone, which results in the pyrolysis of the hydrocarbon feedstock. In this case, pyrolysis refers to pyrolysis of hydrocarbons.
The resulting combustion gas mixture, in which pyrolysis is taking place, then passes through the reaction zone where the carbon black formation reaction is complete.

In another type of furnace carbon black reactor, liquid or gaseous fuel is reacted with an oxidant, preferably air, in the first zone to produce hot combustion gases. These hot gases of combustion pass downstream from the first zone into the reaction chamber and into and through the reaction zone. To produce carbon black, a hydrocarbonaceous feedstock is injected into the passage of the hot combustion gas stream at one or more locations. The hydrocarbonaceous feedstock may be a liquid, gas or vapor and may be the same as or different from the fuel used to produce the hot combustion gas stream. First band (ie
The combustion zone) and the reaction zone may be divided by chokes or zones of limited diameter that are smaller in cross section than the combustion zone or reaction zone. The feedstock may be injected into the passage of hot combustion gases upstream, downstream and / or within the restricted diameter zone. This type of furnace carbon black reactor is generally described in US Reissue Pat. No. 28,974 and US Pat. No. 3,922,335.

Although two types of furnace carbon black reactors and methods have been described, the present invention is directed to any other furnace carbon black reactor or method in which carbon black is produced by pyrolysis and / or incomplete combustion of hydrocarbons. It should be understood that the method could be used.

In both types of processes and reactors described above, and in other generally known reactors and processes, the hot combustion gases effect the pyrolysis of hydrocarbonaceous feedstock injected into the combustion gas stream. The temperature is high enough. In one type of reactor as disclosed in Kester, the feedstock is injected at one or more locations in the same zone where the combustion gases are being produced. In other types of reactors or processes,
Feedstock injection occurs at one or more locations after the combustion gas stream is formed. In both types of reactors, the hot combustion gas stream is continuously flowing downstream in the reactor so that when the mixture of source material and combustion gas passes through the reaction zone, it undergoes thermal decomposition. Occurs continuously. The mixture of feedstock and combustion gases in which pyrolysis has occurred is referred to hereafter as the "effluent". The residence time of the effluent in the reaction zone of the reactor is sufficient under suitable conditions to allow the formation of carbon black. "Residence time" refers to the length of time that has elapsed since the initial contact between the hot combustion gas and the feedstock. After the carbon black having the desired properties is produced, the temperature of the effluent is further reduced to stop pyrolysis. This reduction of the temperature of the effluent to stop the pyrolysis can be done by known methods, such as by injecting a quenching liquid into the effluent through quenching means. As is generally known to those skilled in the art, pyrolysis is stopped when the desired carbon black product is produced in the reactor. One way to determine when pyrolysis should be stopped is by sampling the effluent and measuring its toluene extraction. The amount of toluene extracted is ASTM D1618-83 "Carbon Black Extractables-Tol
uene Discoloration ".
It is generally located where the toluene extraction of the effluent reaches an acceptable amount for the desired carbon black product produced in the reactor. After pyrolysis is stopped, the effluent generally passes through a bag filter system to separate and recover carbon black.

Generally, a single quenching means is utilized. However,
Kester discloses the use of two quenching means to control certain properties of carbon black. Kester relates to adjusting the modulus-imparting properties of carbon black by heat treatment. This heat treatment is performed by adjusting the water flow rate with respect to two water spray quench means arranged in series in the effluent smoke in the carbon black furnace. The modulus of carbon black is related to the performance of carbon black in rubber products. "Effect of He" by Schaeffer and Smith
at Treatment on Reinforcing Properties of Carbon B
lack (effect of heat treatment on the strengthening properties of carbon black) "(Industrial and Engineering Chemistry, 47
Vol. 6, No. 6, June 1955, p. 1286)), heat treatment is generally known to affect the modulus-imparting properties of carbon black. ing. However, as explained further in Schaefer, changes in the modulus-imparting properties of carbon black produced by heat treatment result from changes in the surface chemistry of the carbon black. Therefore, in order to subject the combustion gas streams to different temperature conditions, arranging the quenching means as suggested by Kester, rather than by changing the morphology of the carbon black in some discernable way. By changing the surface chemistry of black, the modulus-imparting properties of carbon black are clearly changed. Furthermore, in Kester both quenching means are arranged in a position in the reaction zone where considerable thermal decomposition of the feed has already taken place. Thus, it is clear that in the Kester method, the characteristics of carbon black CTAB, hue, DBP and Stokes diameter were formed by the time the effluent reached the first quenching means. This supports the conclusion that the change in modulus-imparting properties in Kester does not result from a change in the morphological properties of carbon black. Furthermore, Kester does not place great importance on the position of the first quenching means with respect to the injection position or residence time of the feedstock, and does not disclose means for selecting the position of the first quenching means.

Forseth U.S. Pat. No. 4,230,670 (hereinafter referred to as Forces) suggests two quenching means for stopping pyrolysis. The purpose of the two quenching means is to more completely fill the reaction zone with the quenching liquid to more effectively stop the pyrolysis. However, in Forces, the properties of CTAB, hue, DBT and Stokes diameter of carbon black had been formed by the time the effluent reached the quenching means.

Mills et al. U.S. Pat.No. 4,265,870 and Mills et al. U.S. Pat. No. 4,316,876 use a first quenching means located downstream of the first quenching means to prevent damage to the filter system. Suggest to prevent. In both patents, the first quenching means completely stops pyrolysis, is placed in a position commonly known in the art, and by the time the effluent reaches the first quenching means, the carbon black
The properties of CTAB, hue, DBP and Stokes diameter were formed. The second quenching means further lowers the temperature of the combustion gas stream to protect the filter unit device.

U.S. Pat. No. 4,358,289 to Austin (hereinafter "Oustin") also relates to preventing damage to the filter system by the use of a heat exchanger after quenching. Also, in this patent, the quenching means completely stops pyrolysis and is placed in a position commonly known in the art. In Oustin, characteristics of CTAB, hue, DBP and Stokes diameter of carbon black were formed by the time the effluent reached the first quenching means.

US Pat. No. 3,615,211 to Lewis (hereinafter referred to as Lewis) relates to a method for improving the uniformity of carbon black produced by a reactor and extending the life of the reactor. To improve homogeneity and extend reactor life, Lewis suggests using multiple quenching means arranged throughout the reaction zone to maintain a substantially constant temperature in the reaction zone. ing. A quantity of quench liquid is injected in the quench means located at the most upstream in the reactor, and a larger quantity of quench liquid is injected in each subsequent downstream quench means. The quenching means arranged at the most downstream stops the thermal decomposition. By maintaining a constant temperature in the reaction zone, the Lewis device promotes the uniformity of the carbon black produced by the device. However, the plurality of quenching means do not control the morphology of the carbon black produced by the above device.

However, it is generally desirable to be able to adjust the morphology of the carbon black so that a carbon black suitable for a particular end use can be produced. Also, higher DB
For a given surface area, the increased aggregate size and structure, as represented by P, lower hue, and larger Stokes diameter, makes carbon black well suited for certain end uses. It is desirable to increase the size and structure of aggregates.

[Problems to be Solved by the Invention]

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

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

[Means for Solving the Problems and Action and Effect of the Invention]

The inventors have discovered ways to achieve these desired objectives. The inventors have determined that the temperature of the effluent can be adjusted downstream from the most downstream location of injection of the feedstock to a specific residence time of up to about 0.002 seconds, preferably about 427 ° C. without stopping pyrolysis. It has been discovered that the morphology of the carbon black produced in the furnace carbon black process can be adjusted by lowering the temperature of the effluent further down to 800 ° F) and then further downstream. Lowering the temperature can be accomplished by placing the first quench means downstream and within about 4 feet of the feedstock injection and injecting the quench liquid. According to the present invention, the production of carbon black has a higher DB for a given surface area (CTAB).
It can be adjusted to produce carbon blacks with specific morphological properties as indicated by P, lower hue, and increased Stokes diameter. Moreover, we have found that these morphological properties of carbon black change the amount to which the effluent temperature is reduced and / or reduce the effluent temperature from the time of the most downstream injection of the feedstock. It has been discovered that further control can be achieved by varying the residence time to reach the desired temperature.

More specifically, the present invention determines the temperature of the effluent at the most downstream of the feed injection without stopping the pyrolysis in the effluent (a mixture of combustion gas and feedstock where pyrolysis is occurring). About 0.0 seconds to about 0.002 seconds downstream from the location, preferably about 0 seconds.
It relates to a method for controlling the size and structure of carbon black agglomerates produced by a furnace carbon black reactor by lowering the residence time from 0 to about 0.0015 seconds and then further downstream further reducing the temperature of the effluent. The effluent temperature is approximately 427 ° C (800 ° F) within the specified residence time above.
And more preferably about 10 ° C (50 ° F) to about 427 ° C (800
° F) Can be lowered. The temperature of the effluent can be reduced by quenching means, preferably a quenching means for injecting a quenching liquid into the effluent, located at a predetermined location in the reactor, whereby the effluent can be fed to the feedstock. Quenching downstream from the most downstream location of injection for about 0.0 to 0.02 seconds, preferably about 0.0 to 0.0015 seconds. Typically, in order for the effluent to be quenched within a specified residence time, the quenching means are located within about 1.22 meters (4 feet) of the most downstream location of feedstock injection. The quenching means increases the temperature of the effluent to preferably about 427 ° C (800 ° F), more preferably about 10 ° C (50 ° F).
F) to about 427 ° C (800 ° F), but does not stop pyrolysis. According to the present invention, the amount by which the temperature of the effluent is lowered and the residence time at which the temperature of the effluent takes place can be varied independently or simultaneously and the agglomerates of carbon black produced by the reactor are Adjust the size and structure of. In a reactor that uses quenching means to inject chilled liquid to reduce the effluent temperature within a specified residence time, the amount by which the effluent temperature can be lowered and the effluent temperature drop occur. Such a change in the residence time can be performed by changing the amount of the quench liquid injected from the quenching means and the position of the quenching means, respectively. After the carbon black having the desired properties is produced, the pyrolysis is stopped.

The present invention produces carbon black having a greater aggregate size and structure for a given surface area than a carbon black produced by a similar method in which the effluent temperature is not lowered within a certain residence time. Enables the production of goods.

An advantage of the method of the present invention is that the size and structure of the carbon black aggregates can be controlled.

Another advantage of the present invention is that for a given surface area as shown by CTAB, it has a larger aggregate size and structure as shown by higher DBP, lower hue and increased Stokes diameter. That is, carbon black can be manufactured.

Other advantages of the invention will be apparent from the following description and claims.

[Detailed Description of the Invention]

The figure shows one possible embodiment of the invention. Although a portion of one type of carbon black reactor is shown in the figures, the present invention is directed to any carbon black in which the carbon black is made by pyrolysis and / or incomplete combustion of hydrocarbons. It can be used in a furnace reactor. Further, the following description injects quench liquid to reduce the temperature of the effluent. Embodiments of the invention utilizing quenching means are described, but as will be appreciated by those skilled in the art, the invention is directed to the temperature of the effluent from the location of feed injection closest to the reaction zone within a specified residence time. , Preferably by a specified amount. Similarly, the following description describes the use of a second quenching means to stop the pyrolysis, but as will be appreciated by those skilled in the art, the present invention describes any method for stopping the pyrolysis. Also includes.

In the figure, for example, a portion of a carbon black reactor 10 having a reaction zone 12 and a zone 20 of restricted diameter is
There is provided a first quenching means 40 located at location 60 and a second quenching means located at location 62 for injecting quench liquid 50. The quench liquid 50 may be the same or different for each quench means. Reactor 10,
And the direction of flow of the hot combustion gas stream through zones 12 and 12 is indicated by arrows. The quench liquid 50 is the first quench means.
By means of 40 and the second quenching means 42, injection is carried out countercurrently, or preferably cocurrent, with respect to the direction of the combustion gas flow. place
14 is the most downstream location for injection of feedstock 30. As will be appreciated by those skilled in the art, 14, the most downstream location of feedstock injection, can vary. 14, ie the distance from the most downstream location of feedstock injection to the first quench means location 60 is represented by L-1 and the most downstream location of feedstock injection 14 to the second quench means location. The distance to 62 is L
Represented by -2.

According to the illustrated embodiment of the invention, the first quenching means 60
Lowers the temperature of the effluent (a mixture of combustion gas and feedstock where pyrolysis is occurring) with a residence time of 0.002 seconds or less, preferably 0.0-0.0015 seconds from the most downstream location of feedstock injection Is arranged for. Typically, in order for the effluent to be quenched within a certain residence time, the first quench means will be about 1.22 from the most downstream location of feedstock injection.
Placed within m (4 feet). Therefore, L-1 is about 0.0 m (0.0 ft) to about 1.22 m (4 ft). The temperature of the effluent is preferably in an amount up to 427 ° C (800 ° F), more preferably from about 10 ° C (about 50 ° F) to about 427 ° C (80 ° F).
The quench liquid is injected by the first quench means 60 in order to decrease by an amount of 0 ° F), provided that the quench liquid injected by the first quench means 60 does not stop thermal decomposition.

Furthermore, according to the present invention, the residence time and outflow from the most downstream location of the feedstock injection until the temperature of the effluent (the mixture of combustion gas and feedstock in which pyrolysis occurs) is first reduced. The amount by which the body temperature is lowered can be varied independently or simultaneously and can control the size and structure of the carbon black agglomerates produced by the reactor. In the illustrated embodiment of the invention, varying L-1 changes the residence time from the time of the most downstream injection of feedstock to the time the temperature of the effluent is reduced.
By varying the amount of quench liquid injected, the amount by which the temperature of the effluent can be reduced can be varied.

As mentioned above, in the illustrated embodiment of the invention,
Depending on the aggregate size and structure desired, L-1 typically ranges from about 0.0 m (0.0 ft) to about 1.22 m (about 4 ft). The quenching liquid changes the temperature of the effluent,
Preferably by an amount up to about 427 ° C (800 ° F), more preferably by an amount of about 10 ° C (50 ° F) to about 427 ° C (800 ° F), but the pyrolysis is first quenched by the quench liquid 50. Provided that it is not stopped by means 60.

After the carbon black having the desired properties is produced,
Pyrolysis is stopped at location 62 by quenching means 42. Place 62
Is where carbon black having the desired properties was produced by the reactor. As mentioned above, the location 62 may be determined by any method known in the art for selecting the location of the quenching means to stop pyrolysis. One way to determine the location of the quenching means to stop pyrolysis is by determining where the reaction yields an acceptable amount of toluene extractable for the desired carbon black. The amount of toluene extracted is ASTM test D1618-8.
3 “Carbon Black Extractables-Toluene Discoloratio
It can be measured by using n ". L-2 varies according to the location of location 62.

The effectiveness and advantages of the present invention are further illustrated by the following examples.

〔Example〕

To demonstrate the effectiveness of the present invention, two quenching means are used to vary the residence time from the time of the most downstream injection of feedstock to the time the temperature of the effluent is reduced and the amount by which the temperature of the effluent is reduced. Then, an experiment was conducted by the carbon black manufacturing method. This residence time was changed by changing L-1. The process variables and results of the two sets of carbon black experiments during the experiment are summarized in the table below. Set I
Includes experiments 1, 2, and 3, and set II includes experiments 4, 5, and 6.

Set I: Preheat = 482 ° C (900 ° F; Gas = 7.2kscfh; Air = 80ks
cfh; air / gas = 11.11; primary combustion = 123%; combustion zone capacity = .85ft ³ ; injection zone diameter = 10.7cm (4.2 inches); injection zone length 30cm (12 inches); combustion gas velocity in the injection zone = 609m (2000 feet) / sec; Oil = 125gph; Oil injection pressure = 16.2kg / cm ² gauge pressure (230psig); Oil tip # =
4; Oil tip diameter = 0.107 cm (0.042 inches); Reaction zone diameter = 34.3 cm (13.5 inches) Liquid feedstock (oil)
It had the following composition: H / C ratio = 91; Hydrogen = 6.89% by weight, 7.00% by weight; Carbon = 91.1% by weight, 90.8% by weight; Sulfur = 1.1% by weight; API specific gravity 15.6 / 15.6C (60F) = 5.0; BMC1 (viscosity-specific gravity ) = 141 sets II = preheat = 593 ° C (1100 ° F); gas = 7.5kscfh; air = 80kscfh; air / gas = 106; primary combustion = 118%, combustion zone capacity = .85ft ³ ; injection zone diameter = 10.7 cm (4.2 inches);
Injection Zone Length 30 cm (12 inches); Combustion Gas Velocity in Injection Zone = 701 m (2300 ft) / sec; Oil = 136 gph; Oil Injection Pressure = 19.0 kg / cm ² Gauge Pressure (270 psig); Oil Tip # = 4 Oil tip diameter = 0.107 cm (0.042 inches); Reaction zone diameter = 15 cm (6 inches) The liquid feedstock (oil) had the following composition: H / C
Ratio = 1.06; Hydrogen = 7.99% by weight, 7.99% by weight; Carbon = 89.7
% By weight, 89.5% by weight; Sulfur = 0.5% by weight; API specific gravity 15.6 / 1
5.6C (60F) = 0.5; BMC1 (viscosity-specific gravity) = 123 In both sets I and II, the liquid fuel used for the combustion reaction has a methane content of 95.44% and a wet heat value of 925 BTU / SCF. It was natural gas.

As is generally understood by one of ordinary skill in the art, the process variables shown in the table represent the variables at some location in the reactor and are measured by commonly known methods. Each set of carbon black experiments, with the exceptions listed in the table,
It was carried out in a carbon black reactor similar to the reactor disclosed in Example 1 of US Pat. No. 3,922,335.

In the table, Q represents a quenching means. The first Q foot is L-
1, the distance from the most downstream location of feed injection to the first quenching means. The temperature before the first Q represents the temperature of the effluent before the first quenching means, the temperature after the first quenching means and the temperature after the second quenching means respectively after the first quenching means. It represents the temperature of the effluent and the temperature of the mixture of feed and combustion gas after the second quenching means. All temperatures for quenching are calculated by conventional, well known thermodynamic techniques. The residence times in the table represent the length of time after the most downstream location of feedstock injection that has elapsed before the effluent temperature was first reduced. The second Q foot represents L-2 and was measured experimentally using a toluene extract. After each experiment, the carbon black produced was recovered and analyzed for CTAB, hue, Dst (Medianstokes diameter), C
DBP, Fruity DBP and toluene discoloration were measured. The results of each experiment are shown in the table.

CTAB was measured according to ASTM test procedure D3765-85. Hue was measured according to ASTM test procedure D3265-85a. The DBP of Fruity Black was measured according to the procedure described in ASTM D-2414-86. CDBP was measured according to the procedure described in ASTM D3493-86. Toluene discoloration was measured according to ASTM test procedure D1618-83.

Dst (Means-Stokes Diameter) is a disc centrifuge photosegmentation (photos
edimentometry). The following operation is the I
nstruction Manual for the Joyce-Loebl Disc Centri
fuge, File Ref.DCF 4.008 (issued February 1, 1985),
(Joyce-Loebl Com
pany), (Marquisway, Team Valley, Gateshead, Tyne &
Wear, UK)), and the teachings of this document are incorporated herein by reference. The operation is as follows. A carbon black sample of 10 mg was weighed in a weighing container, and then 0.05% NONIDET P-40 surfactant (NONIDET P-4
0 is a registered trademark of a surfactant manufactured and sold by Shell Chemical Company).
Add to 50 cc of a solution of 10% absolute ethanol, 90% distilled water. This suspension was designated as Sonifier model number.
W385 (New York City, Farmingd
ale) Heat Systems Ultrasonics In
Disperse for 15 minutes with ultrasonic energy using (produced and sold by c.). Prior to the disc centrifuge experiment, the following data is entered into a computer that records the data from the disc centrifuge.

1. Taken as the specific gravity of carbon black, 1.86g / CC.

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

3. The volume of spin liquid, in this case 10 cc of water.

4. Viscosity of the spin liquid, in this case taken as 0.933 centipoise at 23 ° C.

5. Density of spin liquid, in this case 0.9975 g / cc at 23 ° C.

6. Disk speed, in this case 8000 rpm.

7. Data sampling interval, in this case 1 second.

Run the disk centrifuge at 8000 rpm while running the stroboscope. Inject 10 cc of distilled water as a spin liquid into a rotating disk. The turbidity is set to 0 and 1 cc of a solution of 10% absolute ethanol and 90% distilled water is injected as a buffer. The disc centrifuge cut and boost bottoms are then run to create a gentle concentration gradient between the spin liquid and buffer and the gradient is visually monitored. When the gradient becomes gentle, 0.5 cc of dispersed carbon black in aqueous ethanol solution is injected into the spinning disk so that there is no discernable boundary between the two liquids and data collection is started immediately. Stop the experiment when streaming occurs. After injection of dispersed carbon black in aqueous ethanol solution, the disc is rotated for 20 minutes. After 20 minutes of rotation, the disk was stopped, the temperature of the spin liquid was measured, and the average of the temperature of the spin liquid measured at the beginning of the experiment and the temperature of the spin liquid measured at the end of the experiment was recorded from the disk centrifuge. Input to the computer. The data were analyzed according to the standard Stokes equations and are represented using the definitions below.

Carbon black agglomerates-discrete hard colloidal bodies, which are the smallest dispersible units; Stokes diameter-of spheres that settle in a viscous medium in centrifuge or gravity fields according to the Stokes equation diameter. Also, non-spherical objects, such as carbon black agglomerates, can be expressed in terms of Stokes diameter and settling velocity as an object if it is believed to behave as a smooth, hard sphere of the same density. The usual units are expressed as diameter, nm.

Median Stokes Diameter (Dst for recording purposes)
-Points on the Stokes diameter distribution curve when 50% by weight of the sample is larger or smaller. Therefore, it represents the median value of the measurement.

As shown in the table, the present invention provides enhanced CD compared to carbon black produced by control carbon black process runs 1 and 4 using a single quenching means.
Allowed the production of BP, Fruity DBP and Dst and carbon black with reduced hue. This indicates that the carbon black of the present invention is characterized by increased aggregate size and structure. Further, as shown by the results of Set II, the present invention allowed the production of carbon black with increased CDBP, Fruity DBP and Dst and reduced hue for a relatively constant CTAB. . This indicates that the present invention produced carbon black with increased aggregate size and structure for a given CTAB.

As shown by the results of Set I, the present invention was enhanced compared to carbon black produced by Control Carbon Black Process Experiment 1 at different residence times in which the effluent temperature was first reduced by the same amount. CDBP, Fruty
Carbon blacks with DBP and Dst and reduced hue were produced.

Since the present invention relates to a method of controlling the size and structure of carbon black agglomerates, many changes and improvements can clearly be made.

BRIEF DESCRIPTION OF THE DRAWINGS The figure is a cross-sectional view of one embodiment of the present invention in a carbon black reactor, showing the positions of the first and second quenching means. 10 ... Reactor, 12 ... Reaction zone, 40 ... Quenching means, 50 ... Quenching liquid, 60, 62 ... Quenching place.

 ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor William M, Portea USA, Massachusetts, Andover, Bellevue Road 124 (72) Inventor Alancy. Morgan USA, Massachusetts, Manchester, Earl. Old Essex S Road 101 (56) References Japanese Patent Publication Sho 54-13233 (JP, B2)

Claims (10)

[Claims] 1. A stream of hot combustion gas is passed through a reactor and a feedstock is injected into the stream of hot combustion gas at one or more locations to form an effluent and of the feedstock in the effluent. The temperature of the effluent is reduced from the most downstream location of the feedstock injection to 0 downstream without initiating the pyrolysis and stopping the pyrolysis of the feedstock in the effluent.
At a first location within a 002 second period, lowering the temperature of the effluent further at a second location downstream of the first location to stop pyrolysis of the feedstock in the effluent, A method of making carbon black having a controlled aggregate size and structure, which then comprises separating and recovering the carbon black product. 2. The method of claim 1 wherein the temperature of the effluent is reduced by a temperature difference of up to 427 ° C. (800 ° F.). 3. The effluent temperature is about 10 ° C. (50 ° F.) to 427 ° C.
The method of claim 1 wherein the temperature difference is reduced by (800 ° F). 4. The effluent temperature is reduced within a period of 0.0 to 0.0015 seconds from the most downstream location of feedstock injection.
The method described. 5. The effluent temperature is reduced within 0.0 to 0.0015 seconds from the most downstream location of feedstock injection.
The method described. 6. The method of claim 1, wherein the temperature of the effluent is reduced by injecting a quench liquid. 7. The temperature of the effluent is reduced within a period of 0.0 to 0.0015 seconds from the most downstream location of feedstock injection.
The method described. 8. The method of claim 6 wherein the quench liquid lowers the effluent temperature to 427 ° C. (800 ° F.). 9. A quenching liquid raises the temperature of the effluent to 10 ° C. (50 ° F.).
7. The method of claim 6 wherein the temperature is reduced by ~ 427 ° C (800 ° F). 10. The method of claim 7 wherein the quench liquid lowers the effluent temperature by 10 ° C. (50 ° F.) to 427 ° C. (800 ° F.).