KR800001355B1 - Production of carbon blacks - Google Patents

Abstract

Furnace blacks with low structures were prepd. Thus at the 1st stage. such a fuel as methane and an oxidant reacted to form a stream of combustion gases corresponding to a combustion equiv. ratio 1.25 to 0.33, and generate sufficient energy for carbon black formation from hydrocarbons. At the 2nd stage, the fuel gases are injected crosswise into the atream from the 1st stage. At the 3rd phase, the mixt. entered into a reaction zone inwhich oxidant is injected with hydrocarbon for an equivalence ratio of 1.25 to 0.

Description

Manufacturing method of carbon black

The present invention relates to furnace black, which has many important uses, such as fillers, pigments and the like. Most preferably, the method provides a black of semi-reinforcing grades widely used as tire carcass black. In general, the furnace process for producing these carbon blacks involves the pulverization and / or grinding of liquid hydrocarbon feedstocks, such as cyclic feedstocks, in closed transition zones at temperatures above 1800 ° F (about 980 ° C). Incomplete combustion consists in producing carbon black. The carbon black entrained in the gas discharged from the converter is cooled and then collected in a conventional manner. In conventional methods of producing blacks of low structure, such as painted or semi-reinforced carbon blacks, it is very difficult to increase yield without changing the essential properties of the blacks. Moreover, in the conventional method for producing semi-reinforced black, there have been problems such as coke lumps sometimes contained in carbon black products.

It is therefore a primary object of the present invention to provide a new and advanced process for producing carbon blacks that exhibits lower structural properties than carbon blacks produced by methods lacking progress without significantly increasing the particle size of the blacks.

It is another object of the present invention to provide an advanced method of making tire carcass black.

Hereinafter, other objects, advantages and features of the present invention will be described in detail.

According to the present invention, the object of the present invention is to add a portion of the oxidizing agent (e.g. air, etc.) that is generally required in carrying out the reaction to produce the desired carbon black at a position downstream of the point where the hydrocarbon feedstock is It has been found that it can be achieved. Introducing a portion of the oxidant after injecting the raw material in this method results in a lower structure of the resulting black, but does not significantly increase the particle size of the black and may reduce the particle size. In particular, the amount of oxidant introduced downstream is in the range of about 5-45% of the total amount of oxidant required to convert the raw material into the desired carbon black product. The method of injecting the downstream portion of the oxidant into the carbon black containing stream is not critical. For example, the oxidant can be introduced in the circumference, in the longitudinal direction, or in the tangential direction. The downstream addition of the oxidant in the preferred embodiment of the present invention consists of tangential odor. As a result of the downstream injection of the oxidizing agent, not only the structure of the carbon black is lowered, but also the contamination problem of coke and coke lumps accompanying the production of semi-reinforced black in a conventional reactor is reduced, and the yield and Carbon efficiency is about 6-10% higher than conventional methods.

The term "structure" as used herein for carbon black refers to the main properties of carbon black that are not always affected by any property or combination of properties. Generally this term is used to refer to the degree of aggregation of the main particles of black. Since all blacks have some degree of cohesion in their major particles, certain blacks are classified as low, standard, or high structure blacks, depending on their relative degree of cohesion. The classification limits for low, standard, or high structures are generally not clearly defined. It is convenient to regard the black structure as a high structure when the particles tend to form particle chains, while the black structure is considered to be low when the major particles tend to form aggregates. Do. In order to determine the structure of black, the oil absorption method using dibutyl phthalate is used here. This method is performed according to ASTM D-2414-72 and will be described in more detail later.

Although the structural properties of carbon black can be measured directly, a more convenient and reliable method of determining the structural properties of blacks, which is permitted by the art of the art, has been found, which is "dibutyl of carbon black." It is ASTM test method D-2414-72 called "phthalate adsorption water". In brief, this test method uses dibutyl phthalate (OBP) in a fluffy or pelletized carbon black in a Brabender-Cabot Absorptometer (Sawwood Hackensacksey, WW Brabender, New Jersey, USA). After addition to the sample, the volume of dibutyl phthalate used is measured. This value is expressed as the capacity (cm ³ or mm ³ ) of dibutyl phthalate (OBP) relative to 100 g of carbon black. Currently, interrelationships have been established in the art that show the relationship between the structural properties of blacks and the properties of the rubber compositions in which the particular blacks produced are formulated. This relationship is explained as meaning the relationship between the structural degree of black and the elasticity of the rubber composition in which a specific black is blended. In this case, when all other conditions are the same, it is generally recognized that the use of a high structure black produces a high elasticity rubber composition, while the use of a low structure black produces a low elasticity rubber composition. Therefore, in view of the object of the present invention to provide an advanced method for producing a wellness black with significantly lower structural values, the relationship as described above is believed to be correct. In fact, it has been found that incorporation of such blacks in natural and synthetic rubber compositions in the course of producing blacks with significantly lower structural values yields rubber compounds with low elasticity.

In the practice of the present invention particularly suitable for preparing semi-reinforced carbon blacks having iodine adsorbed water in the range of about 28-75 (value measured by ASTM D-1510-70), the following process is carried out.

The liquid feedstock for producing carbon black is injected almost transversely into a pre-generated hot combustion gas stream that flows downstream at an average line speed of at least 500 ft / sec (152.4 m / sec). A raw material sufficient to penetrate into the combustion gas without forming coke on the walls of the carbon formation zone of the reactor is injected transversely from the gas stream into the combustion gas. After the resulting flow is introduced into the reaction zone, the process is injected with the residual oxidant necessary to produce the desired carbon black. As mentioned earlier, the amount of oxidant injected in the reaction zone is in the range of about 5-45% of the total amount of oxidant required to produce the desired carbon black. Oxidizing agents suitable for use in the present invention include air, oxygen, and mixtures of air and oxygen mixed in various concentrations. As a result of applying the improved method of the present invention, the carbon black produced by the present method has significantly reduced its structure without increasing its particle size unduly. The incorporation of the improved black of the present invention into the rubber composition also improved the physical properties of the rubber.

The method of carrying out the invention is described in more detail below.

In producing the hot combustion gas used to produce the black of the present invention, the liquid or gaseous material is reacted in a suitable combustion chamber with a suitable oxidant stream such as air, oxygen, a mixture of air and oxygen, and the like. Suitable fuels for producing hot combustion gases by reacting with oxidants in the combustion chamber are gases, vapors or liquids that can be easily combusted, such as hydrogen, carbon monoxide, methane, acetylene, alcohols, kerosene. However, it is generally preferred to use fuels, especially hydrocarbons, having a high carbon content. Various hydrocarbon gases, including ethane, propane, butane and pentane fractions and fuel oils and flows containing high contents of hydrocarbons such as liquids and rectification by-products, as well as natural gas and reforming or Methane-rich flows, such as concentrated natural gas, can be good fuels. Furthermore, in the first stage of the modular furnace process, it is preferable to use air as the oxidant to generate the primary combustion flame and natural gas as the fuel. The primary combustion rate is then expressed as the amount of oxidant used in the first stage of the Modulus method versus the theoretical amount of oxidant required for the first stage hydrocarbon to be completely burned to produce carbon dioxide and water. Conveniently, this primary combustion rate may be represented in terms of an equivalent ratio instead. Equivalent ratio is defined as the ratio of the supplied fuel to the fuel required to stoichiometrically burn the oxidant. The combustion percentage can be calculated by multiplying the inverse of the equivalent ratio by 100. In the present invention, the primary combustion is in the range of about 1.25-0.33 equivalents, in other words about 80-300% of combustion, in particular about 0.83-0.45 equivalents, ie about 120-220% of combustion. Is preferred.

By this method, a hot stream of combustion gas flowing at a high linear velocity is generated. It has also been found that the pressure difference between the combustion chamber and the reaction chamber is at least 1.0 p.s.i, preferably about 1.5-10 p.s.i. Under these conditions, a gaseous combustion product stream is formed that contains sufficient energy to convert the liquid hydrocarbon feedstock for carbon black production to the desired carbon black. The temperature of the combustion gas stream exiting the primary combustion zone is at least about 2400 ° F. (about 1320 ° C.), most preferably at least about 3000 ° F. (about 1650 ° C.) or more. The hot combustion gas is propagated in one direction at a high linear velocity, and the linear velocity is accelerated by introducing the combustion gas into a closed small diameter transition stage, the diameter of which is usually measured by a venturi throat or the like. Tapered or restricted as necessary by the means. In this method, the step of fiercely injecting the feedstock into the hot combustion gas stream is considered a second step.

In particular, in the second stage where the combustion gas travels on the highway and there is a gas movement pressure of at least 1.0 psi, hot combustion by injecting into the mixed gas under sufficient pressure to desirably infiltrate a suitable liquid hydrocarbon feedstock for carbon black production. High speed mixing and shearing between the gas and the liquid hydrocarbon feedstock is assured. Due to these conditions, the liquid hydrocarbon feedstock is rapidly decomposed and converted to carbon black with high yield. Suitable hydrocarbon feedstocks that can be readily volatilized under these reaction conditions include unsaturated hydrocarbons such as acetylene, olefins such as ethylene, propylene, butylene, aromatic compounds such as benzene, toluene and xylene, certain partially saturated hydrocarbons, kerosene, naphthalenes, Volatile hydrocarbons such as terpenes, ethylene tar, and cyclic aromatic raw materials. When the liquid feedstock is injected almost transversely in the form of a number of small coherent injections from the outer or inner circumference of the hot combustion gas stream or both, the combustion gases will not collide with the jets facing each other. Excellent penetration into the interior or center of the stream. In practicing the present invention, a hydrocarbon feedstock is passed through a plurality of orifices having a diameter of 0.01-0.15 inches, preferably 0.02-0.06 inches, under an injection pressure sufficient to achieve the desired penetration. Can be easily introduced as the liquid interference flow.

The amount of feedstock used is then adjusted according to the amount of fuel and oxidant used so that the total equivalent ratio in the inventive process for producing carbon black can be in the range of at least 6.67-2.50, preferably in the range of about 5.00-3.33. . The total equivalent ratio is defined as the ratio of the total amount of hydrocarbons supplied to the amount of hydrocarbons required for stoichiometric combustion of the oxidant.

The third step of the moduul method includes a reaction zone that allows sufficient residence time for the carbon black formation reaction to occur before the reaction is terminated by quenching. In general the residence time in each case will depend on the specific conditions and the particular black, but the residence time in the process of the invention should be at least 15 milliseconds. Thus, once the carbon black formation reaction has progressed for a predetermined period of time, the reaction is terminated by spraying a quench liquid, such as water, using at least one or more sets of spray nozzles. After passing the hot effluent gas containing the suspended carbon black product downstream, the steps of cooling, separating and collecting the carbon black are carried out according to a conventional method. Separation of carbon black from, for example, a gas stream is readily accomplished by conventional methods such as dust collectors, cyclone separators, large filters or combinations thereof.

Since the structure of the black produced by the modulus method is lowered to some extent, it is found to be useful for applications requiring low structure black. In particular, the structural properties of the black are lowered by introducing about 5-45% of the oxidant of the total oxidant required to produce the desired carbon black into the primary combustion flame in the process after injecting the liquid feedstock. The oxidant is introduced downstream of the reaction zone in the tangential, circumferential or longitudinal direction, with tangential introduction being most preferred. The oxidant introduced downstream may be introduced in the form of the oxidant as it is, or may be introduced in the form of hot combustion gases by reaction with a suitable liquid or gaseous fuel. It has been found that hydrocarbons and oxidants introduced downstream in the present invention may have an equivalent ratio of about 1.25-0, preferably 0.46-0. All of the oxidants or fuels suitable for use in producing the primary combustion flame of the process are also suitable for producing secondary combustion gas streams (ie downstream combustion gas streams). Also, the equivalent ratio in the secondary combustion gas stream is defined the same as in the primary flame, but the equivalent ratio in this secondary combustion gas stream is based on the amount of oxidant used and the amount of oxidant required downstream. The difference is that it is calculated. The oxidants and / or fuels used in the process of the invention are also preferably but not necessarily the same in the production of their combustion gases. In addition, the equivalent ratio of the primary combustion gas stream may be the same as or different from that of the secondary combustion stream downstream. For example, if the flow fuel reacts with an oxidant such as air to produce a primary combustion flame, it is possible to react the natural gas with the oxidant to produce a combustion gas and introduce this combustion gas into the reactor (after injection of the feedstock). In any case, the secondary combustion gas is introduced at a downstream point that will significantly reduce the structure of the resulting carbon black without significantly increasing the particle size of the black.

The following test methods are used to evaluate the analytical and physical properties of the blacks produced by the present invention.

Iodine adsorption water

This iodine adsorbed water is measured according to ASTM D-1510-70.

Iodine Surface Area

인치 깊이까지 버리고, 나머지 블랙 부분의 중량을 측정한다. 이 시료에 0.01N 요오드 용액 100ml를 가하고, 형성된 혼합물을 30분간 교반한다. 이 혼합물 50ml를 용액이 맑아질 때까지 원심분리시킨 후, 종말점 지시약으로서 1% 가용성 전분 용액을 사용하면서 상기 혼합물중의 40ml를 유리 요오드가 흡착될 때까지 0.01N 티오황산 나트륨 용액으로 적정한다. 요오드 흡착 백분율은 블랙 시료를 적정함으로써 정량적으로 측정된다. 그램당 제곱미터(m²/g)의 단위로 표시되는 요오드 표면적은 다음 공식에 의하여 계산된다.The surface area of the fermented carbon black product is measured according to the following iodine adsorption method. In this method, a carbon black sample is placed in a loose lid covered with a loose lid to allow gas to escape, and after cooling for 7 minutes at a temperature of 1700 ° F. (about 930 ° C.) in a muffle furnace, it is cooled. . The top layer of calcined carbon black

Discard to inch depth and weigh the remaining black portion. 100 ml of 0.01 N iodine solution is added to this sample, and the resulting mixture is stirred for 30 minutes. 50 ml of this mixture are centrifuged until the solution is clear, and then 40 ml of the mixture is titrated with 0.01 N sodium thiosulfate solution until free iodine is adsorbed using a 1% soluble starch solution as the endpoint indicator. Iodine adsorption percentage is determined quantitatively by titrating black samples. The iodine surface area, expressed in units of square meters per gram (m ² / g), is calculated by the formula:

This method of measuring the iodine surface area of carbon black pellets has yet to be officially named ASTM, so for convenience it is called Carbot Test Method No. 23.1. Juengel and O'Brien's paper, published in the Cabot Coopulation Publication TG-70-1, issued April 1, 1970, entitled “Industrial Third Black,” The surface area of iodine of Industrial No. 3 Black, measured according to Cabot Test No. 23.1, is 66.5 m ² / g.

Pour density of pelletized carbon black

This test is measured according to ASTM D-1513 and is expressed in units of 1b / ft ³ .

Carbon Black Dibutyl Phthalate Adsorbed Water

This test is measured according to ASTM D-1214-72 as described above. This result can be used to determine whether black is in the form of a feather or a pellet.

Coloring

Coloring power is blended with standard zinc oxide (Florence Green Seal No. 8, produced by New Jersey Jersey Co., Ltd. USA) at a weight ratio of 1: 35.5, and plasticized in the form of epoxidized soybean oil (Rohm & Haas Corporation). After dispersing in production Paraflex G-62), it is expressed as the relative coating power of the pelleted carbon black as compared to a series of standard control blacks tested under the same conditions. In particular, this test involves grinding the carbon black zinc oxide and plasticizer in such a proportion that the final ratio of carbon black to zinc oxide is 1: 37.5. The reflectance is then measured from the film on which the glass plate is located using a Welch Densichron apparatus, and the result is compared with standard carbon black having a known coloring power. The coloring power of the standard carbon black is measured using the coloring power of the Kabot standard SRF carbon black arbitrarily assigned to 100%. In the present invention, Sterling S (Sterling is a registered trademark of Carbot Co., Ltd.) or Sterling R semi-reinforcement varnish black of Carbot Co., Ltd. was used as a standard SRF carbon black having 100% coloration. Each of the Sterling R or String S control blacks has a BET nitrogen surface area of about 23 m ² / g and an oil absorption of about 65-70 lbs oil / 100 lbs black, among other properties, and also has an average particle diameter measured by electron microscopy. It is characterized by 800Å. The only difference is that the Sterling R carbon black is in the form of a feather, while the string S carbon black is in the form of a pellet. Thus, the black selected for control is determined by the state of the black to which the color power is to be measured. Thus, Sterling R or Sterling S semi-reinforced carbon black is considered as the primary control for measuring the coloring power of other blacks.

Another carbon black is used as a control sample to set the color power value in the range of about 30-250% as described above. This is measured in comparison to the primary standard with any 100% color power value. At this time, to provide black as close as possible to the black to be accumulated, a series of contrasting blacks indicating a wide range of coloring power can be used. Examples of carbon blacks used as secondary coloring power standards for this purpose include the following blacks of Carbot Corporation. The analytical values in the following table were measured according to the test methods described herein.

For comparison, the coloring power of Industrial No. 3 Black, measured according to the method described above, is 208% of the first Sterling S semi-reinforced black. These findings appear in Jungel and O'Brien's paper, entitled “Industrial Third Black,” in the Kavot Coopulation Publication TG-70-1, published April 1, 1970.

Modulus and tensile strength

These physical properties are measured according to the ASTM D-412 test method. In short, the elastic modulus measurement is related to the tensile load in lb / in ² units observed when the vulcanized rubber sample is stretched to 300% of its original length. Tensile strength measurements are determined by the number of pounds of tensile load per inch needed to rupture or cut the vulcanized rubber sample in the tensile strength test.

In order that the present invention may be more easily understood, the preparation of representative compounds will be described in detail through the following examples. Of course, there may be other types of the present invention, this embodiment is intended to illustrate the present invention and not intended to limit the present invention.

Example 1

In this embodiment, for example, a means for supplying combustion gas generating reactants such as fuel and oxidant into the primary combustion zone as a separate stream or as a previously burned gaseous reaction product, and a hydrocarbon feed for carbon black production introduced downstream Appropriate reactors were used which provided means for supplying raw materials and combustion gases to the apparatus. The device consists of a suitable material such as metal and consists of a refractory insulator or is surrounded by cooling means such as a recirculating liquid (preferably water). The reactor is also equipped with temperature and pressure recording means such as cooling means for quenching the carbon black formation reaction, means for cooling the carbon black product, means for separating and recovering carbon black from other undesirable by-products, and the like. It is. Therefore, the following method is applied in performing this method. For example, in order to obtain a primary process combustion flame of 141%, i.e. 0.71, preheated air at 700 ° F (about 370 ° C) at a rate of 75.0 mscfh and natural gas at a rate of 5.67 mscfh Filling in the combustion zone of the device through a tube produces a stream of combustion gas flowing downstream at a high linear velocity. Rapidly flowing combustion gas streams are passed through the secondary zone, or transition zone, having a small cross-sectional diameter to increase the linear velocity of the combustion gas streams. Four feed tubes, each 0.055 inch in size, circumferentially positioned for this combustion gas stream, introduce the liquid feedstock almost transversely into the hot combustion gas stream at a rate of 172.1 gallons per hour at 96 psig pressure. The feedstock used in this example (same in all the examples below) has a carbon content of 90.1% by weight, a hydrogen content of 7.96% by weight and a sulfur content of 1.4% by weight, with a hydrogen to carbon ratio of 1.05. , BMCI correlation coefficient of 128, specific gravity of 1.08 according to ASTM D-287, API gravity of -0.7 according to ASTM D-287, SSU viscosity (ASTM D-88) at 130 ° F (54.4 ° C) of 179,210 ° F (98.9). Sunray DX, a fuel with characteristics such as SSU viscosity (ASTM D-88) at 46 ° C. and 46% asphaltene content. The reaction is carried out such that the total combustion rate in the process is 23.3%, i.e. 4.29, and the quench water source to terminate the reaction is located 35 ft (10.7 m) downstream from the feedstock injection point.

Analytical values of black in this example are shown in Table I below. The black of this example is also used as a control for Examples 2 and 3 in which the total amount of oxidant is added to produce the primary combustion flame.

Example 2

According to the method of Example 1, preheated air is charged into the primary combustion zone at a rate of 67.9 m.s.c.f.h. and natural gas at a rate of 5.03 m.s.c.f.h. to produce a 142% or 0.70 equivalent ratio of the primary process combustion flame. The liquid feedstock is introduced through four orifices 0.052 inches in diameter at a rate of 170.7 gallons per hour under a pressure of 129 psig. However, in this embodiment, 9.4% of the total air required to produce the desired black is introduced tangentially into the reaction zone at a rate of 7.1 m.s.c.f.h. at a downstream location where the feedstock is introduced. This air is reacted with the natural gas introduced at a rate of 0.5 m.s.c.f.h. so that the combustion rate of the downstream addition air can be 141%, or 0.71 equivalent ratio, approximately equal to that of the primary flame. The reaction is carried out such that the total combustion rate is 23.5% or 4.26 equivalent ratio, which is quenched with water 35 feet downstream from the point of introduction. Analytical values and physical properties of the black of this example are shown in Table 1 below.

TABLE 1

It is evident from the following examples that the black of the present invention is suitable as a reinforcing agent of the rubber composition. In carrying out the following examples, the rubber composition is easily formulated according to conventional methods. Rubber and carbon black reinforcing agents are well mixed together in conventional mixers commonly used for mixing rubber or plastics, such as Banbury mixers and / or roll mills. The rubber composition is synthesized in accordance with standard industrial production methods for producing materials containing natural and synthetic rubbers. The vulcanized rubber product to be cured is cured at 293 ° F. (145 ° C.) for 15-30 minutes with natural rubber and 35-50 minutes with synthetic rubber (styrene-butadiene in this case).

In evaluating the value of the carbon black of the present invention, the following data are used, and all the amounts indicated are parts by weight.

* All the above data are relative to Industrial No. 4 Black.

The remaining examples were performed according to the method of Examples 1 and 2 except as shown in Table II below.

TABLE II

Table III shows the analysis of the black and the physical properties of natural and synthetic rubber formulations.

TABLE III

* All data for the above rubbers are relative to Industrial No. 4 Black.

While examining the data, the effects of this method will be observed more accurately by comparing Example 1 and Example 2 and Examples 3 and 4, respectively, Examples 5 and 6 and 7. The most remarkable feature of the present invention is that according to the method of the present invention, the structural properties of the carbon black can be reduced without increasing the particle size of the black. Indeed, if the present invention shows any trend, the size of the black particles will appear to be reduced. This is revealed by the overall evaluation of the analytical properties of the blacks produced in the present invention compared to similarly prepared blacks without using the method of the present invention.

From the above data it is shown that almost all other conditions are almost identical, and downstream addition of a portion of the total oxidant required to produce the desired black with the method of the present invention results in a block of the same or slightly smaller particle size. This is indicated by an increase in iodine surface area, coloring power and iodine adsorbed water. The lowering of the structural properties is not only a significant reduction in the DBP adsorbed water, but also an increase in the extrusion shrinkage of the styrene-butadiene rubber composition incorporating black. In general, the process of the present invention produces black which exhibits a decrease in elastic modulus and an increase in tensile strength in natural and synthetic rubber.

In addition, the present invention minimizes the problems that sometimes occur in the conventional process for producing semi-reinforced black, that is, the problem that coke lumps are contained. Another characteristic of the process of the present invention is a 6-12% increase in carbon efficiency compared to the conventional process for producing semi-reinforced blacks.

Example 8

In this example, a more preferred embodiment of the present invention is shown. In this embodiment, the oxidant (air) is reacted with the fuel and introduced downstream in its original form without generating combustion gas. Using only the oxidant as in this embodiment has the advantages of using the oxidant in the form of combustion gas as in the previous embodiments, while being simpler and more economical to operate.

Other hydrocarbon feedstocks are used to carry out this example, ie ethylene process tar, referred to as the English steam cracker bottoms. The ethylene method tar contains 91.2% by weight of carbon, 7.28% by weight of sulfur, 1.2% by weight of sulfur, and a ratio of hydrogen to carbon of 0.95, B.M.C.I. Correlation Coefficient 134, API Gravity according to ASTM D-287 -3.6, Specific Gravity according to ASTM D-287 1.11, SSU Viscosity (ASTM D-88) at 130 ° F (54.4 ° C) of 1000 or more, 210 ° F ( SSU viscosity (ASTM D-88) at 98.9 ° C.) is 106 and the content of asphalen is 19.5%.

According to the method of Example 1, air preheated to 550 ° F. (287.8 ° C.) was charged at a rate of 262.9 mscfh and natural gas at a rate of 14.4 mscfh into the primary combustion zone, yielding an equivalent ratio of 0.52 (ie primary combustion rate of 191). To produce the desired one-stage combustion flame. The ethylene-based tar feedstock is then introduced through six orifices, at a rate of 827 gallons per hour at a pressure of 175 psig, four 0.101 inches in diameter and two 0.089 inches in diameter. Preheated to 550 ° F (287.8 ° C), 18.1% of the total air required to produce the desired black is introduced tangentially into the reaction zone at a rate of 58.1 mscfh downstream of the feedstock feed. Potassium chloride is added at the point of combustion with an overall equivalent ratio of 4.44 (ie 22.5% burn rate) and quenched with water 43ft downstream from the point of introduction. Black was produced in high yield, and the black iodine adsorbed water was 35, the iodine surface area was 28 m ² / g ° C., the coloring power was 121%, and the DBP adsorbed water for the pellet type was 91cc / 100g.

If this example is carried out without adding air downstream, carbon blacks are generally produced which have the same particle size but a much higher structure (DBP). In addition, if potassium chloride is added to lower the structure to an acceptable level when a solid black is produced, a large amount of potassium chloride is required, which eventually increases the coloring power beyond the acceptable level.

In a similar manner, other oxidants such as oxygen or oxygen rich air can also be used successfully in the process of the present invention.

Claims (1)

In the first stage, the fuel and oxidant are reacted to obtain a combustion gas stream having an combustion ratio in the range of about 1.25-0.33 equivalent ratio and containing enough energy to convert the liquid hydrocarbon feedstock for carbon black production to carbon black, Propelling the combustion gas stream at a high linear velocity, the liquid hydrocarbon is injected into the gas stream at a pressure sufficient to achieve the necessary penetration for shearing and mixing in a substantially transverse direction from the surrounding of the combustion gas stream in a number of indirect injection forms. And the resulting downstream gas reaction mixture is sufficient to yield an equivalent ratio of about 1.25-0 to about 5-45% of the total amount of oxidant required to produce the desired carbon black. It is introduced into the third zone, the reaction zone injected with hydrocarbons, and quenched to terminate the reaction and recover carbon black. Fitness carbon black with low structural properties, represented by an increased extrusion shrinkage value of the black-containing rubber composition having a DBP value of less than 6.67-2.50 equivalent ratio and substantially no increase in particle size. The modulus method of making.