WO1989006260A1 - Non-cylindrical reactor for carbon black production - Google Patents
Non-cylindrical reactor for carbon black production Download PDFInfo
- Publication number
- WO1989006260A1 WO1989006260A1 PCT/US1988/003425 US8803425W WO8906260A1 WO 1989006260 A1 WO1989006260 A1 WO 1989006260A1 US 8803425 W US8803425 W US 8803425W WO 8906260 A1 WO8906260 A1 WO 8906260A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- reaction chamber
- die
- carbon black
- hot gas
- hydrocarbon
- Prior art date
Links
Classifications
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
- C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
- C09C1/44—Carbon
- C09C1/48—Carbon black
-
- C—CHEMISTRY; METALLURGY
- C09—DYES; PAINTS; POLISHES; NATURAL RESINS; ADHESIVES; COMPOSITIONS NOT OTHERWISE PROVIDED FOR; APPLICATIONS OF MATERIALS NOT OTHERWISE PROVIDED FOR
- C09C—TREATMENT OF INORGANIC MATERIALS, OTHER THAN FIBROUS FILLERS, TO ENHANCE THEIR PIGMENTING OR FILLING PROPERTIES ; PREPARATION OF CARBON BLACK ; PREPARATION OF INORGANIC MATERIALS WHICH ARE NO SINGLE CHEMICAL COMPOUNDS AND WHICH ARE MAINLY USED AS PIGMENTS OR FILLERS
- C09C1/00—Treatment of specific inorganic materials other than fibrous fillers; Preparation of carbon black
- C09C1/44—Carbon
- C09C1/48—Carbon black
- C09C1/50—Furnace black ; Preparation thereof
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01P—INDEXING SCHEME RELATING TO STRUCTURAL AND PHYSICAL ASPECTS OF SOLID INORGANIC COMPOUNDS
- C01P2006/00—Physical properties of inorganic compounds
- C01P2006/60—Optical properties, e.g. expressed in CIELAB-values
Definitions
- the present invention relates to reactors for the production of carbon black, and more particularly relates to a more efficient carbon black reactor which consistently provides a high-tint carbon black.
- carbon black is produced by injecting a hydrocarbon raw material (hereinafter called "feedstock hydrocarbon") into a flow of hot oxygen-containing gas wherein the feedstock hydrocarbon is partially pyrolyzed before being quenched by a water spray.
- feedstock hydrocarbon a hydrocarbon raw material
- the hot gas is produced by burning a fuel in a combustion chamber.
- the combustion chamber is interconnected axially with a cylindrical reaction chamber and the hot gas produced in the combustion chamber flows through the reaction chamber, where the feedstock hydrocarbon is introduced into the flow of hot gas.
- the feedstock hydrocarbon may be introduced into the flow of hot gas from an axial locus within the reaction chamber, or through the wall of the reaction chamber. It is often preferred to introduce the feedstock hydrocarbon through the wall of the reaction chamber because the axial injection apparatus interferes with the flow of the hot gas from the combustion chamber.
- the feedstock hydrocarbon is pyrolyzed to form carbon black and gaseous by-products. The pyrolysis reaction is then quenched by a spray of water. Finally, the carbon black is separated from the gas flow.
- the physical properties of carbon black may be varied by controlling the process parameters of the carbon black reactor. For example, "tint" is an important property of carbon black. The particle size distribution of the carbon black affects the tint.
- a narrow particle size distribution gives a high-tint carbon black which imparts improved skid and traction qualities to rubber.
- the temperature and amount of the hot gas from the combustion chamber, the amount and distribution of feedstock hydrocarbon in the flow of hot gas, the flow pattern of hot gas and feedstock hydrocarbon through the reactor, the residence time of the feedstock hydrocarbon in the carbon black reactor, the flame length of the pyrolyzing reaction, and the amounts of impurities are parameters that affect the particle size distribution of the carbon black. These process parameters must be controlled in order to control d e particle size distribution of the carbon black product.
- Prior art carbon black reactors generally have cylindrical reaction chambers.
- the temperature and amount of the hot gas from the combustion chamber can be controlled by the amount and type of fuel and the amount of air used for combustion.
- the amount of feedstock hydrocarbon entering the flow of hot gas can be controlled by a simple valve mechanism, but the remaining parameters of the carbon black process can be difficult to control with the cylindrical reactor.
- One way to attempt to control the residence time of d e pyrolyzing feedstock hydrocarbon in die reactor is to move the point of introduction of die feedstock hydrocarbon along the longitudinal axis of d e reaction chamber. The closer the point of introduction of the feedstock hydrocarbon to die combustion chamber, d e longer d e residence time of d e feedstock hydrocarbon.
- die feedstock hydrocarbon When die feedstock hydrocarbon is introduced through the walls of die reaction chamber, the residence time is difficult to control. Moreover, as die feedstock hydrocarbon is introduced dirough die walls of a cylindrical reaction chamber, die feedstock hydrocarbon tends to impinge on the inner surface of die cylindrical reaction chamber around die point of introduction of the feedstock hydrocarbon.
- the temperature of die hot gas within the reaction chamber and tiius the temperature of die curved inner surface of the reaction chamber range from 2000 * Fahrenheit to 3500 * Fahrenheit.
- the temperature of the feedstock hydrocarbon at the point of introduction is generally 350 * Fahrenheit. If die feedstock hydrocarbon is preheated to a much higher temperature it is turned into coke.
- Impingement coke is a hard carbon substance with a particle size much larger tiian high tint carbon black.
- the volume of the reaction chamber becomes increased and consequendy the residence time of the flow of hot gas and pyrolyzing feedstock hydrocarbon becomes increased as die reactor operates.
- This increased residence time provides for more reaction time and tiius alters the panicle size distribution of the carbon black product.
- the presence of refractory grit and impingement coke in the carbon black product also affects the particle size distribution and overall quality of the carbon black. The quality and particle size control thus degrades with time as the conventional cylindrical reactor operates.
- Anodier problem widi die cylindrical prior art carbon black reactors is the inability of the feedstock hydrocarbon sprays to cover the cross sectional area of the hot gas flow when die feedstock hydrocarbon is introduced through die walls of the reaction chamber.
- a non-circular spray pattern is formed.
- the cross section of the cylindrical reactors is circular and, dierefore, the cross section of the hot gas flow through die cylindrical reaction chamber is also circular.
- void hot gas portions of the hot gas flow remain void of feedstock hydrocarbon spray even after d e feedstock hydrocarbon has been introduced.
- the presence of void hot gas has detrimental effects on d e carbon black process.
- die void hot gas increases die flame lengtii of the pyrolyzing feedstock hydrocarbon.
- the flame of the pyrolyzing feedstock hydrocarbon begins with die injection of d e feedstock and ends when die oxygen in d e hot gas flow is consumed. The oxygen remaining in d e void hot gas is not consumed until die oxygen contacts the feedstock hydrocarbon.
- void hot gas over-pyrolyzes some of the feedstock hydrocarbon, diereby broadening die particle size distribution of die carbon black product. Moreover, some of the void hot gas escapes without ever contacting die feedstock hydrocarbon and is wasted.
- d ere is a need for a carbon black reactor which provides greater control over die parameters of die carbon black reaction process and consistendy produces a carbon black wid a narrow particle size range.
- d e reaction chamber of the present invention has a non-circular cross-section and introduces a plurality of hydrocarbon sprays into die reaction chamber to form a non-circular spray pattern at the cross section of die reaction chamber.
- the reaction chamber produces a flow of hot gas having a cross section which conforms substantially to the non- circular cross section of die spray pattern, so as to maximize coverage of die cross sectional area of die hot gas flow by die hydrocarbon spray.
- the reaction chamber of the present invention has an outer shell with a plurality of flat sides defining an inner surface of the reaction chamber.
- the devices for introducing hydrocarbon sprays into the reaction chamber are positioned on the flat sides of the reaction chamber. When the hydrocarbon spray devices are so positioned, the sprays overlap to form a spray pattern wid a cross section which substantially conforms to the cross section of the hot gas flow, thus maximizing coverage of the cross section of the hot gas flow by the hydrocarbon spray.
- the novel construction of the present invention produces a carbon black wid a high tint quality.
- the maximum coverage of die cross sectional area of the hot gas flow by die hydrocarbon spray results in a minimum flame length.
- the minimum flame length causes a uniform pyrolysis of the hydrocarbon spray, which gives a narrow particle size distribution, or high tint, in die carbon black product.
- the maximum coverage of the cross- sectional area of the hot gas flow also eliminates the presence of void hot gas and the waste thereof.
- the novel construction of the present invention provides a carbon black with a consistently reduced impingement of the feedstock hydrocarbon spray.
- the flat sides of the inner surface of the reaction chamber provide a planar surface surrounding die oudet port of each of the hydrocarbon introducing devices so as to substantially eliminate impingement of die hydrocarbon sprays on the inner surface of die reaction chamber, diereby substantially eliminating diermal shock and consequent erosion of die inner surface of the reaction chamber.
- the cross sectional area of the reaction chamber remains constant and consequendy die residence time of die flow of hot gas and pyrolyzing feedstock hydrocarbon remains constant. The constant flow of hot gas and feedstock hydrocarbon provides for greater control over the resulting tint quality of the carbon black product.
- d e impingement of d e hydrocarbon sprays also eliminates die presence of refractory grit and impingement coke in d e carbon black product, which reduces erosion and results in a more narrow and consistent particle size distribution of die carbon black and improves the overall quality of the carbon black.
- Fig. 1 is a sectional longitudinal plan view of the preferred embodiment of die present invention.
- Fig. 2 is an enlarged sectional view taken along line 2-2 of Fig. 1, showing the inner surface of the reaction chamber in the disclosed embodiment
- Fig. 3 is an enlarged schematic section view taken along line 3-3 of die width of die reaction chamber of the disclosed embodiment, illustrating the flow pattern produced by the feedstock hydrocarbon sprays.
- tiiere is shown generally at 10 a carbon black reactor generally comprising a combustion section 12, a reaction chamber 14 connected to die combustion section, a reaction throat 16 connected to an end of the reaction chamber, a plurality of feedstock hydrocarbon injection nozzles 20 entering the reaction chamber and the reaction diroat and an exit chamber 24 connected to an end of the reaction tiiroat
- the combustion section comprises a cylindrical air inlet chamber 26 interconnected axially widi a combustion choke 30.
- the air inlet chamber 26 has an inlet opening 32 for the introduction of a hydrocarbon burner and a second opening for an oxygen-containing gas 33.
- the combustion choke is shown generally at 10 a carbon black reactor generally comprising a combustion section 12, a reaction chamber 14 connected to die combustion section, a reaction throat 16 connected to an end of the reaction chamber, a plurality of feedstock hydrocarbon injection nozzles 20 entering the reaction chamber and the reaction diroat and an exit chamber 24 connected to an end of the reaction tiiroat
- the combustion section comprises a cylindrical
- combustion section 30 is likewise interconnected axially wid a cylindrical combustion chamber 34. It should be understood that the details of the combustion section 12 are known to diose skilled in die art and therefore are not discussed in detail.
- the combustion chamber 34 is interconnected axially with a converging, eight-sided reaction chamber 14.
- the reaction chamber 14 converges in die direction away from the combustion chamber 34.
- the small end 36 of the converging eight-sided reaction chamber 14 is interconnected axially widi an eight-sided reaction diroat 16.
- d e eight-sided reaction chamber The inner surface of d e eight-sided reaction chamber is shown in Fig. 2.
- An important feature of die preferred embodiment is the flat walls
- Feedstock hydrocarbon injection nozzle ports 44 are located on relatively narrow alternating pairs of sides 40a and 40c of the reaction chamber 14 and the corresponding alternating pairs of sides (not shown) of the reaction throat 16.
- the pairs of flat sides 40a and 40c provide a planar surface for the feedstock hydrocarbon injection nozzle ports 44. It is preferable to position the feedstock hydrocarbon injection nozzle ports 44 ' flush with die planar surface of die flat sides 40a and 40c.
- Each feedstock injection nozzle port 44 forms a feedstock hydrocarbon spray with a 90° spray angle.
- the inner surface of the reaction diroat 16 is identical to the cross section of d e reaction chamber 14, except that die reaction throat 16 does not converge.
- the reaction throat 16 is interconnected axially to die exit chamber 24, which has a significantly larger diameter dian die reaction throat 16.
- the carbon black production process begins in the combustion section 12 of carbon black reactor 10 where a hydrocarbon material such as natural gas is mixed with an oxygen-containing gas such as air and combusted. A quantity of oxygen-containing gas in excess of die amount necessary for complete combustion of die hydrocarbon fuel is introduced into die air inlet chamber 26.
- the hot gas produced in die combustion section 12 flows axially through the combustion section towards the reaction chamber 14.
- the temperature of die hot gas generally ranges from 2000" Fahrenheit to 3500" Fahrenheit.
- a feedstock hydrocarbon is sprayed into die flow of hot gas by die injection nozzles 20 tiirough die injection ports 44 located along die walls of die reaction chamber 14 and reaction diroat 16.
- the feedstock hydrocarbon spray is pyrolyzed in the flow of hot gases and forms carbon black particles.
- the carbon black particles suspended in d e flow of hot gas are carried into the exit chamber where die pyrolyzing reaction is quenched by a spray of water (not shown).
- the carbon black particles are dien separated from die flow of gases. It should be understood tiiat d e carbon black product recovery is not a part of this invention and tiius is not discussed in detail.
- planar surfaces of the flat sides 40a and 40c substantially eliminates impingement of die feedstock hydrocarbon on d e inner surface of the reaction chamber 14 that occurs in d e prior art cylindrical reaction chambers as the feedstock hydrocarbon is injected into d e flow of hot gas .
- the elimination of the feedstock hydrocarbon impingement eliminates the thermal shock of the inner surface of the reaction chamber 14 and die consequent erosion of the inner surface of the reaction chamber 14.
- the elimination of die impingement of die feedstock hydrocarbon also eUminates die presence of refractory grit and impingement coke in die carbon black product.
- the dimensions of the reaction chamber cross section (shown in Fig. 3) remain constant and dius d e rate of flow of hot gas tiirough the reaction chamber 14 remains constant. Widi a constant flow rate of hot gas through the reaction chamber 14 and throat 16, the particle size distribution of the carbon black product can be controlled by selecting a particular set of feedstock hydrocarbon injection nozzles 20 along die reaction chamber 14 and throat 16.
- FIG. 3 shows die cross-section of the widdi of the reaction chamber 14 illustrating the flow pattern produced by the feedstock hydrocarbon sprays.
- Each feedstock hydrocarbon injection nozzle 20 forms a feedstock hydrocarbon spray with a 90° spray angle within the reaction chamber.
- a rectangular spray pattern is formed by the overlapping 90 * sprays 46.
- the rectangular pattern of the feedstock hydrocarbon spray substantially conforms to the rectangular cross section of the hot combustion gas flow. As a result, the coverage of the cross sectional area of die flow of hot combustion gas by die feedstock hydrocarbon spray is maximized.
- the maximum coverage of die cross sectional area of die flow of hot combustion gas by die feedstock hydrocarbon provides several advantages over die prior art.
- the flame length of the pyrolyzing feedstock hydrocarbon is r_dnimized.
- the flame is produced by the pyrolysis reaction between the oxygen in die hot gas and the feedstock hydrocarbon spray.
- the flame produced by die pyrolyzing feedstock hydrocarbon ends when all of the oxygen contained in the hot combustion gas is consumed.
- the feedstock hydrocarbon spray covers substantially the entire cross-sectional area of die hot gas flow, substantially all of die oxygen in d e hot gas flow immediately contacts feedstock hydrocarbon as the hot gas flow passes the point of injection of the feedstock hydrocarbon.
- a particular advantage of die minimum flame leng til produced by the carbon black reactor 10 is that the flame of die pyrolyzing feedstock hydrocarbon is kept within the reaction chamber 14 and throat 16, thereby assuring uniform reaction conditions. Because of the large and immediate increase in diameter as die pyrolyzing feedstock enters the exit chamber 24 from the diroat 16, die hot gas undergoes rapid expansion and backmixing. If the flame continues into the exit chamber, the rapid expansion and backmixing causes non-uniform contact of die oxygen in die hot gas with die feedstock hydrocarbon and consequent over-pyrolyzing of portions of the feedstock hydrocarbon.
- Anodier advantage of d e maximum coverage of the cross sectional area of the flow of hot combustion gas is that substantially all of the hot gas produced by die combustion chamber is used in die pyrolyzing reaction, thereby eliminating the waste of any void hot gas tiiat might odierwise escape tiirough die exit chamber 24.
- tiiat the present carbon black reactor is not limited to a reaction chamber and diroat with eight sides, and tiiat reactor chambers and throats with a lesser or greater number of sides are contemplated.
Landscapes
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Pigments, Carbon Blacks, Or Wood Stains (AREA)
Abstract
A non-cylindrical carbon black reactor for consistently and efficiently producing high tint carbon black. A plurality of flat sides defines the inner surface of the carbon black reactor. The flat sides provide a planar surface for the introduction of feedstock hydrocarbon into the reactor, thereby eliminating or substantially reducing impingement of the feedstock hydrocarbon on the inner surface of the reactor chamber and the consequent erosion of the inner surface. The flat sides of the inner surface of the reaction chamber also provide a hot gas flow with a cross-sectional area that substantially conforms to the spray pattern of the feedstock hydrocarbon, thereby providing a minimum flame length within the reactor and a more efficient use of the hot gas.
Description
"NON-CYLINDRICAL REACTOR FOR CARBON BLACK PRODUCTION"
Technical Field
The present invention relates to reactors for the production of carbon black, and more particularly relates to a more efficient carbon black reactor which consistently provides a high-tint carbon black.
Background of the Invention
The basic method for production of carbon black has been known for some time. Generally, carbon black is produced by injecting a hydrocarbon raw material (hereinafter called "feedstock hydrocarbon") into a flow of hot oxygen-containing gas wherein the feedstock hydrocarbon is partially pyrolyzed before being quenched by a water spray. The hot gas is produced by burning a fuel in a combustion chamber. The combustion chamber is interconnected axially with a cylindrical reaction chamber and the hot gas produced in the combustion chamber flows through the reaction chamber, where the feedstock hydrocarbon is introduced into the flow of hot gas.
The feedstock hydrocarbon may be introduced into the flow of hot gas from an axial locus within the reaction chamber, or through the wall of the reaction chamber. It is often preferred to introduce the feedstock hydrocarbon through the wall of the reaction chamber because the axial injection apparatus interferes with the flow of the hot gas from the
combustion chamber. As the flow of hot gas carries the feedstock hydrocarbon, the feedstock hydrocarbon is pyrolyzed to form carbon black and gaseous by-products. The pyrolysis reaction is then quenched by a spray of water. Finally, the carbon black is separated from the gas flow. The physical properties of carbon black may be varied by controlling the process parameters of the carbon black reactor. For example, "tint" is an important property of carbon black. The particle size distribution of the carbon black affects the tint. A narrow particle size distribution gives a high-tint carbon black which imparts improved skid and traction qualities to rubber. The temperature and amount of the hot gas from the combustion chamber, the amount and distribution of feedstock hydrocarbon in the flow of hot gas, the flow pattern of hot gas and feedstock hydrocarbon through the reactor, the residence time of the feedstock hydrocarbon in the carbon black reactor, the flame length of the pyrolyzing reaction, and the amounts of impurities are parameters that affect the particle size distribution of the carbon black. These process parameters must be controlled in order to control d e particle size distribution of the carbon black product.
Prior art carbon black reactors generally have cylindrical reaction chambers. The temperature and amount of the hot gas from the combustion chamber can be controlled by the amount and type of fuel and the amount of air used for combustion. The amount of feedstock hydrocarbon entering the flow of hot gas can be controlled by a simple valve mechanism, but the remaining parameters of the carbon black process can be difficult to control with the cylindrical reactor. One way to attempt to control the residence time of d e pyrolyzing feedstock hydrocarbon in die reactor is to move the point of introduction of die feedstock hydrocarbon along the longitudinal axis of d e reaction chamber. The closer the point of introduction of the feedstock hydrocarbon to die combustion chamber, d e longer d e residence time of d e feedstock hydrocarbon. When die feedstock hydrocarbon is introduced through the walls of die reaction chamber, the residence time is difficult to control. Moreover, as die feedstock hydrocarbon is introduced dirough die walls of a cylindrical reaction chamber, die feedstock hydrocarbon tends to impinge on the inner surface of die cylindrical reaction chamber around die point of introduction of the feedstock hydrocarbon. The temperature of die hot gas within the
reaction chamber and tiius the temperature of die curved inner surface of the reaction chamber range from 2000* Fahrenheit to 3500* Fahrenheit. The temperature of the feedstock hydrocarbon at the point of introduction is generally 350* Fahrenheit. If die feedstock hydrocarbon is preheated to a much higher temperature it is turned into coke. Because of this extreme difference in temperatures, the impingement of die feedstock hydrocarbon on the inner surface of die reaction chamber causes thermal shock to the reaction chamber. The d ermal shock erodes the inner surface of the reaction chamber and widens the cross sectional area of the reaction chamber. The eroded portion of die inner surface of the reaction chamber produces an impurity in the carbon black product called refractory grit. Anodier detrimental effect of die impingement of the feedstock hydrocarbon on the inner surface of the reaction chamber is an impurity called impingement coke, which is a result of the feedstock hydrocarbon contacting the high-temperature surface of die reactor. Impingement coke is a hard carbon substance with a particle size much larger tiian high tint carbon black.
Because of the widened cross section of die reaction chamber due to erosion, the volume of the reaction chamber becomes increased and consequendy the residence time of the flow of hot gas and pyrolyzing feedstock hydrocarbon becomes increased as die reactor operates. This increased residence time provides for more reaction time and tiius alters the panicle size distribution of the carbon black product. The longer the residence time of the feedstock hydrocarbon, die larger the average particle size of die product. The presence of refractory grit and impingement coke in the carbon black product also affects the particle size distribution and overall quality of the carbon black. The quality and particle size control thus degrades with time as the conventional cylindrical reactor operates.
Anodier problem widi die cylindrical prior art carbon black reactors is the inability of the feedstock hydrocarbon sprays to cover the cross sectional area of the hot gas flow when die feedstock hydrocarbon is introduced through die walls of the reaction chamber. When the feedstock hydrocarbon is sprayed into die reaction chamber through the walls of the reaction chamber, a non-circular spray pattern is formed. The cross section of the cylindrical reactors is circular and, dierefore, the cross section of the
hot gas flow through die cylindrical reaction chamber is also circular. Because the non-circular pattern formed by die feedstock hydrocarbon sprays does not match the circular cross section of the hot gas flow, portions (^hereinafter called void hot gas) of the hot gas flow remain void of feedstock hydrocarbon spray even after d e feedstock hydrocarbon has been introduced. The presence of void hot gas has detrimental effects on d e carbon black process. First, die void hot gas increases die flame lengtii of the pyrolyzing feedstock hydrocarbon. The flame of the pyrolyzing feedstock hydrocarbon begins with die injection of d e feedstock and ends when die oxygen in d e hot gas flow is consumed. The oxygen remaining in d e void hot gas is not consumed until die oxygen contacts the feedstock hydrocarbon. This often does not occur until d e void hot gas is further down stream, thus elongating the flame of the pyrolyzing feedstock hydrocarbon. The void hot gas over-pyrolyzes some of the feedstock hydrocarbon, diereby broadening die particle size distribution of die carbon black product. Moreover, some of the void hot gas escapes without ever contacting die feedstock hydrocarbon and is wasted.
Therefore, d ere is a need for a carbon black reactor which provides greater control over die parameters of die carbon black reaction process and consistendy produces a carbon black wid a narrow particle size range.
Summary of the Invention
The present invention solves the above-described problems in the prior art by providing a non-cylindrical reactor for carbon black production. Generally described, d e reaction chamber of the present invention has a non-circular cross-section and introduces a plurality of hydrocarbon sprays into die reaction chamber to form a non-circular spray pattern at the cross section of die reaction chamber. The reaction chamber produces a flow of hot gas having a cross section which conforms substantially to the non- circular cross section of die spray pattern, so as to maximize coverage of die cross sectional area of die hot gas flow by die hydrocarbon spray.
Stated somewhat more specifically, the reaction chamber of the present invention has an outer shell with a plurality of flat sides defining an inner surface of the reaction chamber. The devices for introducing hydrocarbon sprays into the reaction chamber are positioned on the flat
sides of the reaction chamber. When the hydrocarbon spray devices are so positioned, the sprays overlap to form a spray pattern wid a cross section which substantially conforms to the cross section of the hot gas flow, thus maximizing coverage of the cross section of the hot gas flow by the hydrocarbon spray.
The novel construction of the present invention produces a carbon black wid a high tint quality. The maximum coverage of die cross sectional area of the hot gas flow by die hydrocarbon spray results in a minimum flame length. The minimum flame length causes a uniform pyrolysis of the hydrocarbon spray, which gives a narrow particle size distribution, or high tint, in die carbon black product. The maximum coverage of the cross- sectional area of the hot gas flow also eliminates the presence of void hot gas and the waste thereof.
The novel construction of the present invention provides a carbon black with a consistently reduced impingement of the feedstock hydrocarbon spray. The flat sides of the inner surface of the reaction chamber provide a planar surface surrounding die oudet port of each of the hydrocarbon introducing devices so as to substantially eliminate impingement of die hydrocarbon sprays on the inner surface of die reaction chamber, diereby substantially eliminating diermal shock and consequent erosion of die inner surface of the reaction chamber. Without die erosion of the inner surface of die reaction chamber, the cross sectional area of the reaction chamber remains constant and consequendy die residence time of die flow of hot gas and pyrolyzing feedstock hydrocarbon remains constant. The constant flow of hot gas and feedstock hydrocarbon provides for greater control over the resulting tint quality of the carbon black product. The substantial elimination of d e impingement of d e hydrocarbon sprays also eliminates die presence of refractory grit and impingement coke in d e carbon black product, which reduces erosion and results in a more narrow and consistent particle size distribution of die carbon black and improves the overall quality of the carbon black.
Therefore, it is an object of the present invention to provide an improved carbon black reactor.
It is another object of d is invention to provide a carbon black reactor tiiat produces a carbon black widi a consistendy narrow particle size range, or high tint.
It is anodier object of die present invention to provide a carbon black reactor that achieves substantially complete coverage of die cross sectional area of the hot combustion gas by the feedstock hydrocarbon.
It is anodier object of d e present invention to provide a carbon black reactor diat produces a minimum flame lengtii.
It is anodier object of die present invention to provide a carbon black reactor tiiat produces a constant flow of hot combustion gas and feedstock hydrocarbon.
It is anodier object of die present invention to provide a carbon black reactor that substantially reduces or eliminates tiiermal shock and erosion of die inner surface of die carbon black reactor caused by impingement of the feedstock hydrocarbon.
It is anodier object of the present invention to provide a carbon black reactor tiiat substantially reduces or eliminates refractory grit in the carbon black product
It is anodier object of the present invention to provide a carbon black reactor that substantially reduces or eliminates impingement coke in the carbon black product
It is a fuπher object of die present invention to provide a carbon black reactor tiiat substantially reduces or eliminates the waste of hot combustion gases in the production of carbon black. Other objects, features, and advantages will become apparent from reading d e following specifications in conjunction with die accompanying drawings.
*
Brief Description of Drawings Fig. 1 is a sectional longitudinal plan view of the preferred embodiment of die present invention.
Fig. 2 is an enlarged sectional view taken along line 2-2 of Fig. 1, showing the inner surface of the reaction chamber in the disclosed embodiment
Fig. 3 is an enlarged schematic section view taken along line 3-3 of die width of die reaction chamber of the disclosed embodiment, illustrating the flow pattern produced by the feedstock hydrocarbon sprays.
Detailed Description of Preferred Embodiment
Looking first to Fig. 1, tiiere is shown generally at 10 a carbon black reactor generally comprising a combustion section 12, a reaction chamber 14 connected to die combustion section, a reaction throat 16 connected to an end of the reaction chamber, a plurality of feedstock hydrocarbon injection nozzles 20 entering the reaction chamber and the reaction diroat and an exit chamber 24 connected to an end of the reaction tiiroat The combustion section comprises a cylindrical air inlet chamber 26 interconnected axially widi a combustion choke 30. The air inlet chamber 26 has an inlet opening 32 for the introduction of a hydrocarbon burner and a second opening for an oxygen-containing gas 33. The combustion choke
30 is likewise interconnected axially wid a cylindrical combustion chamber 34. It should be understood that the details of the combustion section 12 are known to diose skilled in die art and therefore are not discussed in detail.
The combustion chamber 34 is interconnected axially with a converging, eight-sided reaction chamber 14. The reaction chamber 14 converges in die direction away from the combustion chamber 34. The small end 36 of the converging eight-sided reaction chamber 14 is interconnected axially widi an eight-sided reaction diroat 16.
The inner surface of d e eight-sided reaction chamber is shown in Fig. 2. An important feature of die preferred embodiment is the flat walls
40a, 40b, 40c, and 40d of die reaction chamber 14 shown in Fig. 2. The eight sides of die reaction chamber 14 are positioned in parallel opposing pairs 40a, 40b, 40c and 40d. Feedstock hydrocarbon injection nozzle ports 44 are located on relatively narrow alternating pairs of sides 40a and 40c of the reaction chamber 14 and the corresponding alternating pairs of sides (not shown) of the reaction throat 16. The pairs of flat sides 40a and 40c provide a planar surface for the feedstock hydrocarbon injection nozzle ports 44. It is preferable to position the feedstock hydrocarbon injection nozzle ports 44'flush with die planar surface of die flat sides 40a and 40c.
Each feedstock injection nozzle port 44 forms a feedstock hydrocarbon spray with a 90° spray angle. The inner surface of the reaction diroat 16 is identical to the cross section of d e reaction chamber 14, except that die reaction throat 16 does not converge. The reaction throat 16 is interconnected axially to die exit chamber 24, which has a significantly larger diameter dian die reaction throat 16.
The carbon black production process begins in the combustion section 12 of carbon black reactor 10 where a hydrocarbon material such as natural gas is mixed with an oxygen-containing gas such as air and combusted. A quantity of oxygen-containing gas in excess of die amount necessary for complete combustion of die hydrocarbon fuel is introduced into die air inlet chamber 26. The hot gas produced in die combustion section 12 flows axially through the combustion section towards the reaction chamber 14. The temperature of die hot gas generally ranges from 2000" Fahrenheit to 3500" Fahrenheit. As die hot combustion gas flows axially tiirough the reaction chamber 14 into the reaction diroat 16, a feedstock hydrocarbon is sprayed into die flow of hot gas by die injection nozzles 20 tiirough die injection ports 44 located along die walls of die reaction chamber 14 and reaction diroat 16. The feedstock hydrocarbon spray is pyrolyzed in the flow of hot gases and forms carbon black particles. The carbon black particles suspended in d e flow of hot gas are carried into the exit chamber where die pyrolyzing reaction is quenched by a spray of water (not shown). The carbon black particles are dien separated from die flow of gases. It should be understood tiiat d e carbon black product recovery is not a part of this invention and tiius is not discussed in detail.
The planar surfaces of the flat sides 40a and 40c substantially eliminates impingement of die feedstock hydrocarbon on d e inner surface of the reaction chamber 14 that occurs in d e prior art cylindrical reaction chambers as the feedstock hydrocarbon is injected into d e flow of hot gas .
The elimination of the feedstock hydrocarbon impingement eliminates the thermal shock of the inner surface of the reaction chamber 14 and die consequent erosion of the inner surface of the reaction chamber 14. The elimination of die impingement of die feedstock hydrocarbon also eUminates die presence of refractory grit and impingement coke in die carbon black
product. Without die erosion of die inner surface of d e reaction chamber 14, the dimensions of the reaction chamber cross section (shown in Fig. 3) remain constant and dius d e rate of flow of hot gas tiirough the reaction chamber 14 remains constant. Widi a constant flow rate of hot gas through the reaction chamber 14 and throat 16, the particle size distribution of the carbon black product can be controlled by selecting a particular set of feedstock hydrocarbon injection nozzles 20 along die reaction chamber 14 and throat 16.
Another novel aspect of the carbon black reactor 10 is the substantially rectangular cross section of hot combustion gas produced by d e eight-sided reaction chamber design. Fig. 3 shows die cross-section of the widdi of the reaction chamber 14 illustrating the flow pattern produced by the feedstock hydrocarbon sprays. Each feedstock hydrocarbon injection nozzle 20 forms a feedstock hydrocarbon spray with a 90° spray angle within the reaction chamber. With one set of four feedstock hydrocarbon injection nozzles 20 spraying simultaneously, a rectangular spray pattern is formed by the overlapping 90* sprays 46. The rectangular pattern of the feedstock hydrocarbon spray substantially conforms to the rectangular cross section of the hot combustion gas flow. As a result, the coverage of the cross sectional area of die flow of hot combustion gas by die feedstock hydrocarbon spray is maximized.
The maximum coverage of die cross sectional area of die flow of hot combustion gas by die feedstock hydrocarbon provides several advantages over die prior art. First, by maximizing the coverage of the cross sectional area, the flame length of the pyrolyzing feedstock hydrocarbon is r_dnimized. The flame is produced by the pyrolysis reaction between the oxygen in die hot gas and the feedstock hydrocarbon spray. The flame produced by die pyrolyzing feedstock hydrocarbon ends when all of the oxygen contained in the hot combustion gas is consumed. When the feedstock hydrocarbon spray covers substantially the entire cross-sectional area of die hot gas flow, substantially all of die oxygen in d e hot gas flow immediately contacts feedstock hydrocarbon as the hot gas flow passes the point of injection of the feedstock hydrocarbon. As a result, substantially all of the oxygen quickly and uniformly reacts with the feedstock hydrocarbon and die flame ends. This aspect of d e present carbon black
reactor prevents the undesirable consequences of void hot gas, which otherwise occurs when less than full coverage of the cross sectional area of die hot gas flow is obtained (as with die cylindrical reactor). Consequently, the present reactor avoids over-pyrolyzing some of the feedstock hydrocarbon and maintains a desirable narrow particle size distribution of die carbon black product
A particular advantage of die minimum flame leng til produced by the carbon black reactor 10 is that the flame of die pyrolyzing feedstock hydrocarbon is kept within the reaction chamber 14 and throat 16, thereby assuring uniform reaction conditions. Because of the large and immediate increase in diameter as die pyrolyzing feedstock enters the exit chamber 24 from the diroat 16, die hot gas undergoes rapid expansion and backmixing. If the flame continues into the exit chamber, the rapid expansion and backmixing causes non-uniform contact of die oxygen in die hot gas with die feedstock hydrocarbon and consequent over-pyrolyzing of portions of the feedstock hydrocarbon. Anodier advantage of d e maximum coverage of the cross sectional area of the flow of hot combustion gas is that substantially all of the hot gas produced by die combustion chamber is used in die pyrolyzing reaction, thereby eliminating the waste of any void hot gas tiiat might odierwise escape tiirough die exit chamber 24.
It should be understood that increased coverage of the cross sectional area of the hot gas flow and resulting benefits can be obtained to varying degrees with feedstock hydrocarbon spray angles between 30° and 120° . At broader angles it is necessary for the feedstock hydrocarbon injection nozzles to extend beyond the inner surface of the reactor so the feedstock hydrocarbon spray does not impinge on the inner surface as the feedstock hydrocarbon is injected.
It should also be understood tiiat the present carbon black reactor is not limited to a reaction chamber and diroat with eight sides, and tiiat reactor chambers and throats with a lesser or greater number of sides are contemplated.
It should further be understood tiiat d e foregoing relates only to a preferred embodiment of die present invention, and that numerous changes and modifications therein may be made witiiout departing from the spirit and scope of die invention as defined in the following claims.
Claims
1. Apparatus for the production of carbon black, comprising: means for producing a flow of hot gas; a reaction chamber having an inlet opening receiving the flow of hot gas and having an outlet opening so that the hot gas can flow through the reaction chamber, means for introducing a plurality of hydrocarbon sprays into the reaction chamber between the inlet opening and die oudet opening of the reaction chamber to form a non-circular spray pattern at a cross-section of die reaction chamber, and means in the reaction chamber producing a cross-section of said flow of hot gas which conforms substantially to the cross-section of die spray pattern, so as to maximize coverage of the cross-sectional area of the hot gas flow by die hydrocarbon spray.
2. Apparatus for the production of carbon black, comprising: means for producing a flow of hot gas; a reaction chamber having an outer shell; the outer shell having a plurality of flat sides defining an inner surface of the reaction chamber, the reaction chamber also having an inlet opening receiving the flow of hot gas and an outlet opening so that the hot gas can flow through the reaction chamber, means for introducing a plurality of hydrocarbon sprays into the reaction chamber on the flat sides of die reaction chamber between the inlet opening and die oudet opening of die reaction chamber to form a non- circular spray pattern at a cross-section of die reaction chamber; and the reaction chamber inner surface defined by the flat sides producing a cross-section of the flow of hot gas which conforms substantially to the cross-section of the spray pattern so as to maximize coverage of the cross- sectional area of the hot gas flow by the hydrocarbon spray.
3. An apparatus for the production of carbon black as in Claim 2 wherein: the plural hydrocarbon sprays each have a predetermined spray angle, and the sprays overlap to form the spray pattern.
4. An apparatus for the production of carbon black, as in claim 2 wherein: the flat sides are even in number, each of the flat sides is positioned in substantially parallel and opposing pairs; and die means for introducing a plurality of hydrocarbon sprays into die reaction chamber are positioned on alternate flat sides of th& reaction chamber.
5. An apparatus for the production of carbon black as in claim 4, wherein: die flat sides are eight in number.
6. An apparatus for the production of carbon black as in claim 5 wherein: the plural hydrocarbon sprays are four in number, each having a spray angle between 30* and 120*.
7. An apparatus for die production of carbon black as in claim 6 wherein: each of die hydrocarbon sprays a have a spray angle of substantially 90*; and the sprays overlap to form a spray pattern of substantially rectangular cross-section.
8. An apparatus for the production of carbon black comprising: means for producing a flow of hot gas; a reaction chamber having an outer shell; the outer shell having a plurality of flat sides defining an inner surface of die reaction chamber, the reaction chamber also having an inlet opening receiving the flow of hot gas and an outlet opening so tiiat the hot gas can flow through the reaction chamber, means for introducing a plurality of hydrocarbon sprays into the reaction chamber, each of the hydrocarbon introducing means having an outlet port on the flat sides of die reaction chamber between the inlet opening and the outlet opening of the reaction chamber, and the flat sides providing a planar surface surrounding the outlet port of each of the hydrocarbon introducing means so as to substantially reduce impingement of the hydrocarbon sprays on the inner surface thereby substantially reducing thermal shock and consequent erosion of the inner surface of the reaction chamber.
9. The apparatus for production of carbon black as in claim 8, wherein: the outlet port of each hydrocarbon introducing means is positioned flush with the inner surface of the reaction chamber.
Priority Applications (6)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
IN803/CAL/88A IN169714B (en) | 1988-01-11 | 1988-09-26 | |
AU25436/88A AU617710B2 (en) | 1988-01-11 | 1988-10-06 | Non-cylindrical reactor for carbon black production |
BR888807385A BR8807385A (en) | 1988-01-11 | 1988-10-06 | APPARATUS FOR THE PRODUCTION OF BLACK SMOKE |
EP88909030A EP0368936B2 (en) | 1988-01-11 | 1988-10-06 | Non-cylindrical reactor for carbon black production |
KR1019890700658A KR940003962B1 (en) | 1988-01-11 | 1988-10-06 | Non-cylidrical reactor for carbon black production |
DE3873342T DE3873342T3 (en) | 1988-01-11 | 1988-10-06 | NON-CYLINDRICAL REACTOR FOR THE PRODUCTION OF FURNACE Soot. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US07/142,478 US4927607A (en) | 1988-01-11 | 1988-01-11 | Non-cylindrical reactor for carbon black production |
US142,478 | 1988-01-11 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO1989006260A1 true WO1989006260A1 (en) | 1989-07-13 |
Family
ID=22499997
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/US1988/003425 WO1989006260A1 (en) | 1988-01-11 | 1988-10-06 | Non-cylindrical reactor for carbon black production |
Country Status (15)
Country | Link |
---|---|
US (1) | US4927607A (en) |
EP (1) | EP0368936B2 (en) |
JP (1) | JPH0774315B2 (en) |
KR (1) | KR940003962B1 (en) |
AU (1) | AU617710B2 (en) |
BR (1) | BR8807385A (en) |
CA (1) | CA1306599C (en) |
DE (1) | DE3873342T3 (en) |
ES (1) | ES2006674A6 (en) |
IN (1) | IN169714B (en) |
MX (1) | MX164224B (en) |
NZ (1) | NZ227571A (en) |
PH (1) | PH24827A (en) |
PT (1) | PT89418B (en) |
WO (1) | WO1989006260A1 (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1994014899A1 (en) * | 1992-12-23 | 1994-07-07 | Kvaerner Engineering A.S | A method and device for the pyrolytic decomposition of hydrocarbons |
US8002856B2 (en) | 2006-01-20 | 2011-08-23 | Ineos Europe Limited | Process for contracting a hydrocarbon and an oxygen-containing gas with a catalyst bed |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2624115B1 (en) * | 1987-12-03 | 1990-04-13 | Gaz De France | PROCESS AND APPARATUS FOR CONVERSION OF HYDROCARBONS |
DE69735235T2 (en) | 1996-05-16 | 2006-07-27 | Columbian Chemicals Company | ROUGH FOR MOTOR VEHICLES AND THE COMPOSITIONS CONTAINING THEM |
FR2760182B1 (en) * | 1997-02-28 | 1999-04-16 | Minna From Finland | IMPROVING SHOWERS AND SHOWER ENCLOSURES |
JP4643790B2 (en) * | 2000-03-15 | 2011-03-02 | 旭カーボン株式会社 | Carbon black manufacturing apparatus and manufacturing method |
JP3859057B2 (en) * | 2001-06-22 | 2006-12-20 | 旭カーボン株式会社 | Carbon black production equipment |
US7238741B2 (en) | 2004-05-13 | 2007-07-03 | Columbian Chemicals Company | Carbonaceous material with broad aggregate size distribution and improved dispersibility |
US20060034748A1 (en) * | 2004-08-11 | 2006-02-16 | Lewis David R | Device for providing improved combustion in a carbon black reactor |
DE102007047432A1 (en) | 2007-10-04 | 2009-04-09 | Evonik Degussa Gmbh | Carbon black, process for its preparation and its use |
RU2011119468A (en) * | 2008-10-16 | 2012-11-27 | Эвоник Карбон Блэк Гмбх | SOOT, METHOD OF ITS PRODUCTION AND ITS APPLICATION |
EP2563864B1 (en) * | 2010-04-27 | 2020-07-08 | Aditya Birla Science and Technology Company Private Limited | Carbon black reactor |
EP2623564A1 (en) | 2012-02-03 | 2013-08-07 | Omya International AG | Installation for the purification of minerals, pigments and/or fillers and/or the preparation of precipitated earth alkali carbonate |
Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB977622A (en) * | 1961-07-07 | 1964-12-09 | Lynco Ltd Of Panama S A | Carbon black |
DE2507021B2 (en) * | 1974-02-25 | 1978-12-21 | Cabot Corp., Billerica, Mass. (V.St.A.) | Process for the production of carbon black |
US4391789A (en) * | 1982-04-15 | 1983-07-05 | Columbian Chemicals Company | Carbon black process |
Family Cites Families (34)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CA827569A (en) * | 1969-11-18 | E. Dollinger Robert | Method and apparatus for producing carbon black | |
CA842123A (en) * | 1970-05-19 | Kraus Gerard | Production of carbon black | |
CA811653A (en) * | 1969-04-29 | E. Dollinger Robert | Production of furnace carbon black | |
CA828064A (en) * | 1969-11-25 | Phillips Petroleum Company | Method and apparatus for producing carbon black | |
CA876015A (en) * | 1971-07-20 | J. Gunnell Thomas | Method of carbon black production | |
CA827577A (en) * | 1969-11-18 | J. Forseth Glenn | Production of carbon black | |
CA911684A (en) * | 1972-10-10 | Charles R. Venable, Jr. | Carbon black reactor | |
CA835289A (en) * | 1970-02-24 | Phillips Petroleum Company | Method and apparatus for producing carbon black | |
CA811058A (en) * | 1969-04-22 | Phillips Petroleum Company | Method and apparatus for producing carbon black | |
CA828065A (en) * | 1969-11-25 | J. Gunnell Thomas | Production of carbon black | |
CA821460A (en) * | 1969-08-26 | H. Kallenberger Robert | Method and apparatus for producing carbon black | |
US2705190A (en) * | 1951-07-31 | 1955-03-29 | Columbian Carbon | Apparatus for carbon black manufacture |
US2769692A (en) * | 1952-05-06 | 1956-11-06 | Columbian Carbon | Carbon black process and apparatus |
US3490869A (en) * | 1966-11-17 | 1970-01-20 | Columbian Carbon | Vortex reactor for carbon black manufacture |
US3490870A (en) * | 1967-08-09 | 1970-01-20 | Columbian Carbon | Method and apparatus for the production of carbon black |
US3563706A (en) * | 1967-12-29 | 1971-02-16 | Phillips Petroleum Co | Production of carbon black |
US3522005A (en) * | 1968-02-28 | 1970-07-28 | Cities Service Co | Process and apparatus for manufacture of carbon black |
US3592597A (en) * | 1968-05-23 | 1971-07-13 | Phillips Petroleum Co | Carbon black process and reactor |
CA928936A (en) * | 1968-12-30 | 1973-06-26 | Phillips Petroleum Company | Large size carbon black producing process and product |
US3787562A (en) * | 1969-01-02 | 1974-01-22 | Cities Service Co | Carbon blacks having improved dispersion and platewear characteristics |
BE758008A (en) * | 1969-10-27 | 1971-04-26 | Phillips Petroleum Co | PROCESS FOR OBTAINING CARBON BLACK |
US3867513A (en) * | 1970-01-08 | 1975-02-18 | Phillips Petroleum Co | Method for producing carbon black |
US3615210A (en) * | 1970-04-02 | 1971-10-26 | Cabot Corp | Process for production of carbon black |
US3726964A (en) * | 1970-11-18 | 1973-04-10 | Phillips Petroleum Co | Process for the production of carbon black |
CA967724A (en) * | 1970-12-31 | 1975-05-20 | Robert E. Dollinger | Production of simulated lamp black |
US3832450A (en) * | 1972-12-18 | 1974-08-27 | Cities Service Co | Carbon black process |
US3988478A (en) * | 1974-02-22 | 1976-10-26 | Cities Service Company | Carbon black |
US4195068A (en) * | 1974-03-06 | 1980-03-25 | Deutsche Gold- Und Silber-Scheideanstalt Vormals Roessler | Process for the production of furnace black |
US3959008A (en) * | 1974-06-24 | 1976-05-25 | Cities Service Company | Carbon black |
FR2321713A1 (en) * | 1975-08-22 | 1977-03-18 | Danel Francois | UNDERWATER VIEWING DEVICE |
CH630948A5 (en) * | 1977-09-02 | 1982-07-15 | Mura Anst | SOOT PRODUCTION PLANT. |
US4283378A (en) * | 1979-08-01 | 1981-08-11 | Cabot Corporation | Production of high surface area carbon blacks |
US4370308A (en) * | 1981-05-15 | 1983-01-25 | Cabot Corporation | Production of carbon black |
US4342736A (en) * | 1981-06-01 | 1982-08-03 | Columbian Chemicals Company | Reduction of the degradation of refractories in a carbon black reactor |
-
1988
- 1988-01-11 US US07/142,478 patent/US4927607A/en not_active Expired - Lifetime
- 1988-09-26 IN IN803/CAL/88A patent/IN169714B/en unknown
- 1988-10-05 CA CA000579410A patent/CA1306599C/en not_active Expired - Lifetime
- 1988-10-06 KR KR1019890700658A patent/KR940003962B1/en not_active IP Right Cessation
- 1988-10-06 WO PCT/US1988/003425 patent/WO1989006260A1/en active IP Right Grant
- 1988-10-06 AU AU25436/88A patent/AU617710B2/en not_active Ceased
- 1988-10-06 DE DE3873342T patent/DE3873342T3/en not_active Expired - Fee Related
- 1988-10-06 BR BR888807385A patent/BR8807385A/en not_active IP Right Cessation
- 1988-10-06 EP EP88909030A patent/EP0368936B2/en not_active Expired - Lifetime
- 1988-10-14 JP JP63257472A patent/JPH0774315B2/en not_active Expired - Lifetime
-
1989
- 1989-01-09 NZ NZ227571A patent/NZ227571A/en unknown
- 1989-01-09 MX MX14467A patent/MX164224B/en unknown
- 1989-01-10 PT PT89418A patent/PT89418B/en not_active IP Right Cessation
- 1989-01-10 PH PH38025A patent/PH24827A/en unknown
- 1989-01-10 ES ES8900073A patent/ES2006674A6/en not_active Expired
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB977622A (en) * | 1961-07-07 | 1964-12-09 | Lynco Ltd Of Panama S A | Carbon black |
DE2507021B2 (en) * | 1974-02-25 | 1978-12-21 | Cabot Corp., Billerica, Mass. (V.St.A.) | Process for the production of carbon black |
US4391789A (en) * | 1982-04-15 | 1983-07-05 | Columbian Chemicals Company | Carbon black process |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO1994014899A1 (en) * | 1992-12-23 | 1994-07-07 | Kvaerner Engineering A.S | A method and device for the pyrolytic decomposition of hydrocarbons |
US5989512A (en) * | 1992-12-23 | 1999-11-23 | Kvaerner Technology And Research Ltd. | Method and device for the pyrolytic decomposition of hydrocarbons |
US8002856B2 (en) | 2006-01-20 | 2011-08-23 | Ineos Europe Limited | Process for contracting a hydrocarbon and an oxygen-containing gas with a catalyst bed |
Also Published As
Publication number | Publication date |
---|---|
IN169714B (en) | 1991-12-14 |
CA1306599C (en) | 1992-08-25 |
PT89418A (en) | 1989-10-04 |
EP0368936B2 (en) | 1998-11-11 |
PT89418B (en) | 1994-01-31 |
AU617710B2 (en) | 1991-12-05 |
EP0368936A1 (en) | 1990-05-23 |
EP0368936B1 (en) | 1992-07-29 |
PH24827A (en) | 1990-10-30 |
AU2543688A (en) | 1989-08-01 |
BR8807385A (en) | 1990-03-20 |
JPH028259A (en) | 1990-01-11 |
KR900700549A (en) | 1990-08-16 |
US4927607A (en) | 1990-05-22 |
NZ227571A (en) | 1990-06-26 |
MX164224B (en) | 1992-07-27 |
KR940003962B1 (en) | 1994-05-09 |
JPH0774315B2 (en) | 1995-08-09 |
DE3873342T2 (en) | 1993-03-25 |
DE3873342D1 (en) | 1992-09-03 |
ES2006674A6 (en) | 1989-05-01 |
DE3873342T3 (en) | 1999-04-22 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US4391789A (en) | Carbon black process | |
US4927607A (en) | Non-cylindrical reactor for carbon black production | |
KR0166972B1 (en) | Method and apparatus for producing carbon black | |
US4228131A (en) | Apparatus for the production of carbon black | |
USRE28974E (en) | Process for making carbon black | |
US3498753A (en) | Apparatus for thermal cracking of hydrocarbon | |
CA1300343C (en) | Apparatus and process for producing carbon black | |
US3701827A (en) | Process and apparatus for the production of large particle-size,low structure carbon black | |
KR0181521B1 (en) | Carbon black manufacturing method | |
JP2013527278A (en) | Carbon black reactor | |
US3431075A (en) | Production of carbon black | |
EP1093493B1 (en) | Process and apparatus for producing carbon blacks | |
US4339422A (en) | Carbon black manufacture | |
US3060003A (en) | Process and apparatus for producing carbon black | |
US5256388A (en) | Method for consistently producing carbon black having a high tint | |
US4970059A (en) | Method of producing furnace carbon black | |
US5069882A (en) | Carbon black reactor with a choke extension | |
US3565586A (en) | Apparatus for producing carbon black | |
US3563706A (en) | Production of carbon black | |
US3607065A (en) | Production of carbon black | |
US3322506A (en) | Carbon black apparatus | |
US4446108A (en) | Carbon black manufacture | |
US3475125A (en) | Production of carbon black | |
US4051135A (en) | Carbon black reactor | |
US4826669A (en) | Method for carbon black production |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
WWE | Wipo information: entry into national phase |
Ref document number: 1988909030 Country of ref document: EP |
|
AK | Designated states |
Kind code of ref document: A1 Designated state(s): AU BR KR |
|
AL | Designated countries for regional patents |
Kind code of ref document: A1 Designated state(s): DE FR GB IT NL SE |
|
WWP | Wipo information: published in national office |
Ref document number: 1988909030 Country of ref document: EP |
|
WWG | Wipo information: grant in national office |
Ref document number: 1988909030 Country of ref document: EP |