US2782101A - Manufacture of carbon black - Google Patents

Manufacture of carbon black Download PDF

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Publication number
US2782101A
US2782101A US243020A US24302051A US2782101A US 2782101 A US2782101 A US 2782101A US 243020 A US243020 A US 243020A US 24302051 A US24302051 A US 24302051A US 2782101 A US2782101 A US 2782101A
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United States
Prior art keywords
chamber
hydrocarbon
gases
blast
oxygen
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Expired - Lifetime
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US243020A
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English (en)
Inventor
George L Heller
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Columbian Carbon Co
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Columbian Carbon Co
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Publication date
Application filed by Columbian Carbon Co filed Critical Columbian Carbon Co
Priority to US243020A priority Critical patent/US2782101A/en
Priority to DEC6313A priority patent/DE975285C/de
Application granted granted Critical
Publication of US2782101A publication Critical patent/US2782101A/en
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Expired - Lifetime legal-status Critical Current

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    • 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

Definitions

  • the present invention relates to the manufacture of furnace black and, more, particularly, to a process of the type involving the thermal decomposition of a hydrocarbon by rapidly, uniformly mixing it with a hot gaseous medium at a temperature in excess of that at which the hydrocarbon is decomposed to carbon black.
  • the present invention is directed primarily to improvements in processes of the type-described in said application whereby the yield of carbon black may be substan:
  • a particularly desirable aspect of the process of said application is the operation thereof in which the hydrocarbon make is a heavy, high molecular weight material containing large proportions of aromatic constituents, for instance, heavy hydrocarbon fractions or residuum resulting from the cracking of petroleum to produce 7 motor fuel.
  • the present invention is particularly applimixture. should contain a proportion of oxygen such as results inan oxidizing blast flame. Where smaller proportions of oxygen, or air, are used, one is apt to experience flare backsj into the burnerports, unless the. hydrocarbon injection nozzlesof the blast burners are advanced to a position where theyare subject to rapid destruction by radiant heat from the furnace chamber.
  • suflicient to combine with the active oxygen or oxidiztioned at different distances from the block 3.
  • I may use a flue gas pref,- erably hot, containing substantial proportions of hydrogen for combiningwith the oxidizingcomponents of the blast flame gases or I may use other material in the form of; gas, or vapor, which will combine withwthose oxidizing components to form gaseous reaction products which may be readily separated fromvthe carbon black.
  • I may use for this purpose aninexpensive grade of natural gas, "or other low molecular weight hydrocarbons, or I may use substantially pure hydrogen, where such is economically available.
  • This oxygen.- scavenger i.
  • reducing agent e., reducing agent
  • the combustion zone of the reaction chamber separately from the combustible mixture supplied through the blast ports in such a way that it will become intimately admixed with the oxidizing blast flame gases before the oxidizing constituents of those gases can consume or otherwise react with the-radially injected hydrocarbon make.
  • Figure 2 is a transverse section of the reaction chamber along the line 2-2 of Figure 1; and y Figure 3 is a transverseasection of the reaction chamher along the line 3-.-3 of Figure 1 showing moreclearly the arrangement of hydrocarbon make injection nozzles.
  • the numeral 1 indicates a cylindrical reaction chamber, one end of which opens into the vertical cooler 2.
  • the reaction chamber opens into a somewhat enlarged conibustion'c'hamber 1a which is closed at its upstream end by a block of refractory material 3 through which pipe 4 extends axially, 'through which the blast burnersrnay be ignited and which, when not. in use, is normally closed by the cap 4a.
  • the chamber 1 is delineated. by the cylindrical wall 5 of highly refractory material which, in turn, is covered by a second layer of furnace refractory 6 which also delineates the combustion chamber 1a.
  • This outer layer of refractory material is covered by layer 7' of heat-insulating material.
  • Extending through the layers of refractory and heat-insulating material forming the furnace side wall, substantially perpendicular to the longitudinal axis of the chamber are four blast burners 8, each entering the combustionchamber in a circumferential or tangential direction, as more clearly shown in Figure 2 of the drawings.
  • the apparatus shown ispro vided with two identical sets of these blast burners posi- In operation, only one or both sets of the burners may be used as desired,.or one or more burners of the separate sets may'beused.
  • the furnace chamber' isprovided with a' set of four radiallydirectedhydrocarbon make injection nozzles 9, spaced apart and extending through the furnace sidewall, as more clearly shown in Figure 3' of the drawings.
  • These nozzles are provided for the injection into the furnace chamber of liquid hydrocarbon to be decomposed and are normally positioned with their inner ends substantially flush with the inner wall of the furnace chamber;
  • the present invention is independent of the particular type of nozzle used, the
  • Hydrocarbon fuel is supplied to the blast burners through valved tubes 12 projecting axially through the respective burner ports and terminating short of the inner wall of the combustion chamber.
  • Air for combustion is forced by any suitable means through the conduit 1-3 and introduced tangentially into the annularduct 14, as more clearly shown in Figure 2 of the drawing, each set of blast burners being equipped with a separate air duct.
  • the outer ends of the burner ports 8 open into the air ducts 14 and, advantageously, are shaped, as shown in the drawing, to utilize the whirling of the air in the duct to facilitate the directing of the air through the respective ports.
  • a combustible mixture of the air supplied through conduit 13 and the hydrocarbon fuel supplied through tubes 12 is tangentially injected at high velocity into the combustion chamber'and is burned therein to form a swirling cyclone of blast flame gases passing longitudinally through the reaction chamber.
  • - Liquid hydrocarbon make is radially injected into this swirling body of hot gases through the spray nozzles 9 and is substantially instantaneously mixed therewith and is decomposed by heat absorbed therefrom to form carbon black in suspension in the furnace gases.
  • the resultant suspension of carbon black in furnace gases flows from the reaction chamber and upwardly through the vertical cooler 2 wherein the suspension is cooled by contact with water sprays 24. Any unvaporized water from these sprays, together with any carbon knocked out of suspension, passes downwardly from the vertical cooler into the sump 25 and the cooled suspension passes from the upper end of the vertical cooler through conduit 26 to conventional separating and collecting apparatus as is wellunderstood by the art.
  • the oxygen-scavenger is mixed with these hot blast flame gases prior to the mixing of the hydrocarbon make therewith/This may be accomplished by introducing the oxygen-scavenger into theupstream end of the combustion chamber by any suitable means, for instance, through the tube 4, or where only one set of blast burners is being used, the oxygen-scavenger may be introduced through one or more burners of the other set, no oxygen being supplied to the burner ports through which the oxygen-scavenger is introduced.
  • the optimum proportion of the oxygen-scavenger to be used is dependent upon other operating conditions and should, of course,be increased with an increase in the oxidizing characteristics of the blast flame gases.
  • the proportion of oxygen-scavenger will also depend upon the capacity of the scavenger to reactwith, or neutralize, the oxidizing constituents of the blast flame gases.
  • a hydrocarbon gas for instance, natural gas of the type charged to the blast burners
  • oxygen scavenger l have found that ratios of air to total gas, i. e., fuel gas plus auxiliary gas or oxygen scaven-
  • i 4 is readily determined by simple flue gas analysis-under the particular operating conditions prevailing.
  • sufi'icient auxiliary gas it is generally advantageous to introduce sufi'icient auxiliary gas to bring ,the total amount of gas introduced, i. e. fuel gas plus auxiliary gas, to a proportion such that about 85% to 90% theoretically complete combustion is effected. This will usually require a ratio of air to total gas within the range of about 9.311 to 9.8:1.
  • auxiliary gasis to scavenge not only excess free oxygen but also further to reduce any oxidizing components of the blast flame gases, for instance, CO2 and water vapor, in order to retard or minimize robber side reactions which tend to reduce the yield of carbon black per unit of hydrocarbon make.
  • sufficient auxiliary gas should be used to effect a reduction of the oxidizing components of the blast flame gases to an extentsuch that the CO2 content of the resultant gases is within the range of about 4.5% to 10%, the CO content is within the range of about 9.5% to 3%, the 02 content does not exceed about /z% and no appreciable amount of illuminant is present.
  • the hydrocarbon make was a so-called pressure tar obtained by the thermal cracking of cycle stock from a catalytic cracking operation.
  • the hydrocarbon make was a residuum obtained from the straight thermal cracking of an aromatic crude. Both of these materials are highly aromatic.
  • Example IX I In an operation carried on in apparatus similar to that just described, to which air was supplied through the blast burners at the rate of 180,000 cubic feet per hour and a fuel gas of 1020 B. t. u. value and which theoreticallyrequired an air-gas ratio of 10.6:1 for combustion tially increased over that obtained by operations under comparable conditions, except that the scavenger gas was not employed.
  • Example X In operations carried on in similar apparatus, using fuel gas of the type used in Example IX and to which air was supplied at the rate of 180,000 cubic feet per hour, the ratio of air to fuel gas being 11.8 and hydrocarbon make being introduced at the rate of 162 gallons per hour, I have, with advantage, introduced axially into the combustion chamber auxiliary gas of the same type as the fuel gas at the rate of 4500 cubic feet per hour, and obtained yields of carbon black equivalent to 4.85 pounds per gallon of the hydrocarbon make.
  • heavy hydrocarbons such as fuel oil #5, #6, or Bunker C and products known to the trade as pressure tar, or flash drum tar" characterized by high aromat icity, low pour point, and high specific gravity.
  • Preferred tars of this type are those having A. P. 1. values from to -6, SSU fural viscosities at 122 F. of from 125 to 250, and which are soluble in pentachlorphenol and have specific gravities of from 0.95 to 1.1. These products are readily available from most refineries using thermal cracking methods.
  • these heavy tars are preheated to about 250 F. or as required to reduce the viscosity for atomization, but not to exceed 500 F.
  • Another efiicacious procedure is to dilute the heavy residuum products with an aromatic cycle stock to secure the desired pour point.
  • hydrocarbon make is a tar-like hydrocarbon obtained by the thermal cracking of cycle stock from a catalytic cracking operation.
  • hydrocarbon make is a heavy high molecular weight hydrocarbon residue resulting from the cracking of petroleum and comprising 20%-95% by weight of aromatic constituents.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Hydrogen, Water And Hydrids (AREA)
US243020A 1951-08-22 1951-08-22 Manufacture of carbon black Expired - Lifetime US2782101A (en)

Priority Applications (2)

Application Number Priority Date Filing Date Title
US243020A US2782101A (en) 1951-08-22 1951-08-22 Manufacture of carbon black
DEC6313A DE975285C (de) 1951-08-22 1952-08-23 Verfahren zur Herstellung von Ofenruss

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US243020A US2782101A (en) 1951-08-22 1951-08-22 Manufacture of carbon black

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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1083001B (de) * 1957-07-11 1960-06-09 Columbian Carbon Verfahren und Vorrichtung zur Herstellung von Aktivruss
US2985511A (en) * 1958-09-29 1961-05-23 Columbian Carbon Carbon black manufacture
US3051556A (en) * 1960-04-11 1962-08-28 United Carbon Company Inc Carbon black apparatus
US3175888A (en) * 1961-05-29 1965-03-30 Phillips Petroleum Co Apparatus for producing low structure carbon black
US3490869A (en) * 1966-11-17 1970-01-20 Columbian Carbon Vortex reactor for carbon black manufacture
US4299797A (en) * 1977-09-19 1981-11-10 Phillips Petroleum Company Carbon black production
US4490346A (en) * 1982-07-12 1984-12-25 Phillips Petroleum Company Method for producing carbon black
US4540560A (en) * 1982-08-30 1985-09-10 Phillips Petroleum Company Carbon blacks
US4765964A (en) * 1983-09-20 1988-08-23 Phillips Petroleum Company Carbon black reactor having a reactor throat
US4859426A (en) * 1982-07-12 1989-08-22 Phillips Petroleum Company Apparatus for producing carbon black
US11453584B2 (en) 2018-06-29 2022-09-27 Palo Alto Research Center Incorporated High throughput methane pyrolysis reactor for low-cost hydrogen production

Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1811854A (en) * 1928-04-19 1931-06-30 Columbian Carbon Manufacture of carbon black
US1844327A (en) * 1928-10-27 1932-02-09 Standard Oil Co Process and apparatus for manufacturing lamp black
US2106137A (en) * 1934-07-09 1938-01-18 Forrest C Reed Process of producing carbon black
US2144971A (en) * 1936-06-27 1939-01-24 Gen Atlas Carbon Company Manufacture of carbon black
US2375795A (en) * 1941-12-22 1945-05-15 Phillips Petroleum Co Carbon black process
US2378055A (en) * 1942-06-27 1945-06-12 Columbian Carbon Manufacture of carbon black
US2440424A (en) * 1944-05-04 1948-04-27 Columbian Carbon Manufacture of carbon black
US2499438A (en) * 1944-09-12 1950-03-07 Columbian Carbon Manufacture of carbon black
US2564736A (en) * 1947-03-08 1951-08-21 Cabot Godfrey L Inc Process of producing carbon black
US2599981A (en) * 1949-12-22 1952-06-10 Columbian Carbon Carbon black
US2623811A (en) * 1949-11-16 1952-12-30 Huber Corp J M Process for producing carbon black and valuable by-product gases

Family Cites Families (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2375796A (en) * 1942-02-16 1945-05-15 Phillips Petroleum Co Process of making carbon black
GB699406A (en) * 1949-04-19 1953-11-04 Cabot Godfrey L Inc Process and apparatus for the production of carbon black

Patent Citations (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1811854A (en) * 1928-04-19 1931-06-30 Columbian Carbon Manufacture of carbon black
US1844327A (en) * 1928-10-27 1932-02-09 Standard Oil Co Process and apparatus for manufacturing lamp black
US2106137A (en) * 1934-07-09 1938-01-18 Forrest C Reed Process of producing carbon black
US2144971A (en) * 1936-06-27 1939-01-24 Gen Atlas Carbon Company Manufacture of carbon black
US2375795A (en) * 1941-12-22 1945-05-15 Phillips Petroleum Co Carbon black process
US2378055A (en) * 1942-06-27 1945-06-12 Columbian Carbon Manufacture of carbon black
US2440424A (en) * 1944-05-04 1948-04-27 Columbian Carbon Manufacture of carbon black
US2499438A (en) * 1944-09-12 1950-03-07 Columbian Carbon Manufacture of carbon black
US2564736A (en) * 1947-03-08 1951-08-21 Cabot Godfrey L Inc Process of producing carbon black
US2623811A (en) * 1949-11-16 1952-12-30 Huber Corp J M Process for producing carbon black and valuable by-product gases
US2599981A (en) * 1949-12-22 1952-06-10 Columbian Carbon Carbon black

Cited By (13)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE1083001B (de) * 1957-07-11 1960-06-09 Columbian Carbon Verfahren und Vorrichtung zur Herstellung von Aktivruss
US2985511A (en) * 1958-09-29 1961-05-23 Columbian Carbon Carbon black manufacture
US3051556A (en) * 1960-04-11 1962-08-28 United Carbon Company Inc Carbon black apparatus
US3175888A (en) * 1961-05-29 1965-03-30 Phillips Petroleum Co Apparatus for producing low structure carbon black
US3490869A (en) * 1966-11-17 1970-01-20 Columbian Carbon Vortex reactor for carbon black manufacture
US4299797A (en) * 1977-09-19 1981-11-10 Phillips Petroleum Company Carbon black production
US4490346A (en) * 1982-07-12 1984-12-25 Phillips Petroleum Company Method for producing carbon black
US4859426A (en) * 1982-07-12 1989-08-22 Phillips Petroleum Company Apparatus for producing carbon black
US4540560A (en) * 1982-08-30 1985-09-10 Phillips Petroleum Company Carbon blacks
US4765964A (en) * 1983-09-20 1988-08-23 Phillips Petroleum Company Carbon black reactor having a reactor throat
US11453584B2 (en) 2018-06-29 2022-09-27 Palo Alto Research Center Incorporated High throughput methane pyrolysis reactor for low-cost hydrogen production
US11964867B2 (en) 2018-06-29 2024-04-23 Xerox Corporation High throughput methane pyrolysis reactor for low-cost hydrogen production
US11981563B2 (en) 2018-06-29 2024-05-14 Xerox Corporation High throughput methane pyrolysis reactor for low-cost hydrogen production

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