US2441613A - Method and apparatus for pulverizing and processing materials - Google Patents

Method and apparatus for pulverizing and processing materials Download PDF

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US2441613A
US2441613A US471266A US47126643A US2441613A US 2441613 A US2441613 A US 2441613A US 471266 A US471266 A US 471266A US 47126643 A US47126643 A US 47126643A US 2441613 A US2441613 A US 2441613A
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chamber
vortex
gases
combustion
vortex chamber
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Balassa Ladislaus
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2/00—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic
    • B01J2/16—Processes or devices for granulating materials, e.g. fertilisers in general; Rendering particulate materials free flowing in general, e.g. making them hydrophobic by suspending the powder material in a gas, e.g. in fluidised beds or as a falling curtain
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C19/00—Other disintegrating devices or methods
    • B02C19/06—Jet mills
    • B02C19/061—Jet mills of the cylindrical type
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/10—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers
    • F26B17/107—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by fluid currents, e.g. issuing from a nozzle, e.g. pneumatic, flash, vortex or entrainment dryers pneumatically inducing within the drying enclosure a curved flow path, e.g. circular, spiral, helical; Cyclone or Vortex dryers
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B17/00—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement
    • F26B17/24—Machines or apparatus for drying materials in loose, plastic, or fluidised form, e.g. granules, staple fibres, with progressive movement with movement performed by shooting or throwing the materials, e.g. after which the materials are subject to impact
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F26—DRYING
    • F26B—DRYING SOLID MATERIALS OR OBJECTS BY REMOVING LIQUID THEREFROM
    • F26B3/00—Drying solid materials or objects by processes involving the application of heat
    • F26B3/02—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air
    • F26B3/10—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour carrying the materials or objects to be dried with it
    • F26B3/12—Drying solid materials or objects by processes involving the application of heat by convection, i.e. heat being conveyed from a heat source to the materials or objects to be dried by a gas or vapour, e.g. air the gas or vapour carrying the materials or objects to be dried with it in the form of a spray, i.e. sprayed or dispersed emulsions or suspensions

Definitions

  • My invention relates to a method and apparatus for pulverizing and activating material at high temperatures
  • pulverizing methods and apparhtus utilizing compressed air hish pressure steam or other similar forms of fluid energy to create a vortex have been proposed and successfully employed.
  • Such pulverizers usually consist of a circular or cylindrical vortex chamber into which the gaseous fluid is injected through one or more jets placed in such a manner as to create a vortex and to maintain the gaseous fluid in a spiralling vertex in the chamber.
  • the material to be treated is introduced into the vortex at its periphery, and the cyclonic or tornado-like vortex of the gases sublects the entrained material to the combined effects of powerful centrifugal forces, as well as of friction and impact, both of the particles on each other and on the walls of the chamber, resulting in the reduction of the particle size of said material to a flne powder.
  • the prior art contemplate the use of fluids at high temperature, such as above 800 F., or any other change than a reduction in the particle size of the materials being treated.
  • My invention has as an object the utilization of high temperature. high velocity gaseous fluid for pulverizing and reacting with the material at high temperature.
  • a further object is a method by which material suspended in a gaseous medium may be pulverized and calcined simultaneously.
  • Another object is a method and apparatus suitable for simultaneously grinding and reducing oxide ores to metal.
  • a further object is a method and apparatus suitable for the drying of wet mineral pigment pulps, thus avoiding th formation of hard agglomerates which necessitate further grinding.
  • An even further object is a method and apparatus by which materials in solution may be dried in an eiilclent manner. Other objects will appear hereinafter.
  • these objects may be accomplished by the continuous combustion of suitable fluid fuel-air blends in a pressure combustion chamber under uniform pressure.
  • the heat energy in the burned gases is converted into velocity by expansion, and the gases are discharged into a vortex chamber, in such a manner as to create and maintain a high velocity inwardly spiralling vortex.
  • the gases are discharged from the center of the vortex into a reaction chamber, retaining to a large extent both their velocity and their spiral movement.
  • the material to be treated having a mesh size not greater than inch but verize said material.
  • the eflect obtained by my methods and in my apparatus in addition to reduction in the particle size, may be that of calcination, drying, oxidation and chemical reduction, depending on the material being treated and on the composition of the gases employed.
  • Figure l is a vertical section of an apparatus suitable for the carrying out of my invention.
  • FIG. 2 is a horizontal fragmentary section of the same apparatus
  • Figure 3 is a diagrammatic plan view of a modified form.
  • the apparatus is provided with a combustion chamber I that has a heat resistant lining ii.
  • a combustion chamber I Leading into the chamber I is a compressed air inlet pipe 2 connected to the venturi ill and leading into the mouth of the venturi is a fluid fuel inlet nozzle 3.
  • the combustion chamber I is provided with an ignition plug 4 in one of the walls for igniting the fuel.
  • the exit end of the chamber l is constricted to form a nozzle 5 which is connected with and tangent to the disc-shaped vortex chamber 6, the latter in turn being connected with and leading into the cylindrical reaction chamber ll of relatively smaller diameter.
  • the chamber II is provided on its inner'side with a spiral baifle l3 extending from the bottom to the top of chamber II, and is connected at the outlet end with the duct l2 which leads to any suitable collecting or treating apparatus.
  • I For feeding the material to be treated into the apparatus, I provide a hopper I with an injector feeder head 9 opening into the vortex chamber 0, a compressed air or steam supply pipe 8 being connected to the feeder head.
  • the chambers a and ii may be provided with a water or steam jacket ls-having an intake l6 and outlet I6.
  • the bottom of the vortex chamber is also provided with a baflle l3a.
  • la and lb are combustion chambers, similar to combustion chamber l of Figs. 1 and 2 in structure and arrangement. These chambers lead into the vortex chamber 6a and the products of that chamber are led from the center of the chamber 8a to the periphery of a similar central part of the vortex chamber 6b by the conduit 20. From the vortex chamber 6b, the gases are conducted through the spiral reaction chamber I lb and out the duct lib, all as in Fig. 1.
  • the fluid Leaving the vortex chamber 6 through the center of the vortex, the fluid enters the reaction chamber ll. Retaining a considerable part of its rotative or spiralling motion the fluid proceeds through the reaction chamber II which is equipped with a spiral baflle l3 which aids in maintaining the rotative motion of the fluid.
  • the material to be treated is forced through the injector feeder head 9 into the vortex chamber 6. Under the combined efi'ects of the high heat oi. the combustion gases, of the centrifugal forces created by the high velocity vortex, of the friction and impact between the particles of the material and of the walls of the vortex chamber, the material is rapidly disintegrated to a fine powder.
  • the centrifugal force keeps the larger particles near the periphery of the vortex while the smaller, finely ground particles are carried by the inwardly spiralling gaseous fluid into the reaction chamber.
  • the material While being pulverized and in the reaction chamber, the material is subjected not only to the physical forces of heat, friction and impact but also to the chemical action of the gaseous fluid.
  • the gaseous fluid exerts one of the following three eifects:
  • the eflect In the case of complete combustion of the fuel, with no excess oxygen present, the eflect is usuglluyd only that of the heat transmitted by the If a high fuelratio is used, leaving an excess of fuel in pa ial stages of combustion, the eifect of the fluid is strongly reducing.
  • the treated material, entrained in the fluid may be precipitated, either in cyclone separators utilizing the vertical energy still remaining or collected by settling in flues, by filtering with cloth,'or by magnetic or electrostatic means.
  • the water and steam jackets ll around the reaction and vortex chambers serve to protect the walls of the apparatus from the high heat of the gaseous fluid as well as to capture part of the waste heat.
  • the steam produced in the jackets may be used to generate the power necessary for the operation of the process.
  • my invention is readily adaptable for the treating of materials in a variety of ways hitherto unobtainable in vortex grinding apparatus.
  • I By adjusting the fuel-air ratio in the combustion chamber I, so as to provide air in a slight excess over that theoretically required for the particular fuel used, I am able to obtain temperatures as high as 2500 F. in the vortex chamber. Under these conditions.
  • my invention is particularly suited for the simultaneous grinding and calcination of materials. Under such conditions, I have fed a water wet mineral pigment pulp into the vortex chamber and obtained a product which was dried. finely pulverized and calcined as well.
  • the gases entering the vortex chamber in this case contained a high percentage of carbon monoxide, some free carbon, hydrogen and methane.
  • the chemical effect of the gases was strongly reducing while the temperature obtained was between 1800 and 2000 F. Under these conditions I am able to reduce iron oxide ore (hematite) to metal.
  • the volume of the combustion chambers l was about 4 gallons each with nozzles 5 of A.” diameter, the vortex chamber 6 had a diameter of 38" and a height of 5 3" measured from inside to inside of the base plate and the top at the periphery of the vortex chamber.
  • the reaction chamber l I had an inside diameter of 24" and a height of ten feet.
  • the injector feeder head 9 had a nozzle with a opening and the venturi opening of A" in diameter at its narrowest part.
  • Example 1 Air at a pressure of 40 lbs. per square inch'was I introduced into the combustion chamber. Fuel oil was introduced at first in sufiicient amount to obtain complete combustion. After the combustion chamber became sufficiently hot to support combustion, the fuel-air ratio was adjusted to the Example 2 Using air at a pressure of 40 lbs. per square inch and only the minimum of fuel, with which continuous combustion could be maintained, a gaseous fiuid with highly oxidizing character was obtained. When coarse iron sulfide ore (pyrites) was introduced into the vortex chamber. iron oxide having an average particle size of two microns was collected in the fines.
  • Example 3 Example 4 The conditions of Example 3 were maintained in this experiment. When a 50% solution of ferric sulfate (coquimbite) in water was fed into the vortex chamber, finely pulverized iron oxide was recovered from the centrifugal separator.
  • ferric sulfate coquimbite
  • Example 5 The conditions of Example 3 were maintained in this experiment, but the apparatus was changed to have the vortex chamber'l in vertical position, and the reaction chamber I I in horizontal position. When a mixture of 2 mols of sodium carbonate and one mol of silica was fed into the vortex chamber, fused sodium meta-silicate was obtained from the centrifugal separator.
  • Example 6 The conditions of Example 3 were maintained in this experiment. When a water wet pulp of acid treated barium sulfate containing 30% water was fed into the vortex chamber, a highly calcined and finely pulverized product of good white color was obtained.
  • Example 7 The conditions of Example 5 were maintained in this experiment, using hydrogen as fuel. When a 25% solution of sodium hydroxide in water was fed into the vortex chamber, fused sodium hydroxide of around 90% NaOH content was obtained from the centrifugal separator.
  • Example 8 The conditions of Example 3 were maintained in this experiment. When a mixture of calcium carbonate and silica in equi-molecular proportions was fed into the vortex chamber finely pulverized calcium silicate was obtained from the centrifugal separator.
  • the apparatus if desired may be constructed of metal or of suitable ceramic materials,
  • the combustion chambers may be of any suitable design or shape and are preferably lined with fire brick.
  • the nozzle 0 should preferably be of quartz or other similar heat resisting material.
  • the glow plug 4 may be of any of the standard designs used in Diesel engines or it may be substituted by a spark plug or glow wire.
  • I have utilized the gaseous fluid obtained through continuous combustion of a fuel-air mixture under pressure. Satisfactory results may be obtained, however, also if the fluid is produced through intermittent combustion or through successive explosions of the fuel-air mixture and irrespective of whether the fuel-air mixture was compressed before ignition or if it was ignited at atmospheric pressure.
  • Any of the conventional combustible fuels meeting the above requirements may be employed, such as furnace oil, Diesel oil, kerosene, illuminating, natural and water gas, hydrogen. butane and the like and powdered coal.
  • the operating pressure in the combustion chamber may range from 30 lbs. per square inch up, depending on the construction of the apparatus.
  • the pressure in the vortex and reaction chambers will usually be near atmospheric but it may reach substantially higher pressures.
  • High pressures are used when the vortex chambers are hooked up in tandem, as shown in Fig. 3, for the gradual stepwise expansion of the gases.
  • the most useful range of operating temperatures will lie between 1000-1800 C. in the combustion chamber, and between 800-1400 C. in the vortex and reaction chambers, although high temperatures are operative in both chambers.
  • the speed of the vortex is above 20,000 R. P. M. and preferably about 40,000 R. P. M.
  • reaction chamber may be lengthened to any extent necessary to obtain a retention time sumcient for the completion of the reaction in question.
  • Both the vortex and the reaction chamber may be equipped with jets suitable for the iniectlon of air, steam or other gases to modify the quality a of the product obtained.
  • the direction of the reaction may be changed from oxidation to reduction or vice versa by changing the composition of the gases at various stages. For instance, calcining in the first stage with a slight excess of air and then in the second stage introducing a reducing gas like methane or ethyl alcohol, which after exhausting the excess oxygen provides a strong reducing atmosphere.
  • a reducing gas like methane or ethyl alcohol
  • a method of pulverlzing solid material and simultaneously chemically reacting said material at high temperatures comprising the steps of leading a combustible mixture into a combustion chamber and burning the same under conditions which create high temperatures and pressures in said chamber, leading the combustion gases from said combustion chamber through a narrow passageway to a circular vortex chamber and introducing the combustion gases from said passageway tangentially into said circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, simultaneously cooling the vortex chamber and introducing the gases into a reaction chamber which conducts the material and gases through a prolonged path in the reaction chamber whereby slowing down of the gases is effected and causes substantial completion of said reaction.
  • a method of pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising the steps of leading a-combustible mixture into a combustion chamber and burning the same under conditions which create high temperatures and pressures in said chamber, leading the combustion gases from said combustion chamber through a narrow passageway to a-circular vortex chamber and introducing the combustion gases from said passageway tangentially into said circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, simultaneously cooling the vortex chamber and introducing the gases into a reaction chamber which conducts the material and gases through a spiral path in the reaction chamber whereby slowing down of the gases is eflected and causes substantial completion of said reaction.
  • a method of pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising the steps of leading a combustible mixture into a combustion chamber and burning the same under conditions which create high temperatures and pressures in said chamber, leading the combustion gases from said combustion chamber through a narrow passageway while simultaneously cooling said passageway at a point adjacent to its connection to said vortex chamber and introducing the combustion gases from said passageway tangentially into a circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, simultaneously cooling the vortex chamber and introducing the gases into a reaction chamber which conducts the material. and gases through a prolonged path in the reaction chamber whereby slowing down 01' the gases is eflected and causes substantial completion of said reaction.
  • An apparatus for memeverizing solid material and simultaneously chemically reacting said material at high temperatures comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including at least one nozzle angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to. its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber axially mounted as to said vortex chamber and axially communicating therewith, said reaction chamber being constructed to provide an elongated path of flow for the mixture of gas and solid particles and to prevent direct straight line flow therethrough.
  • An'apparatus for pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including at least one nozzle angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber, means mounting said reaction chamber above and axially aligned as to said vortex chamber and axially communicating therewith, said reaction chamber being constructed to provide an elongated path of flow for the mixture of gas and solid particles and to prevent direct straight line flow therethrough.
  • An apparatus for pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including at least one nozzle angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber axially mounted as to said vortex chamreaction chamber being constructed to provide a 10 ber and axially communicating therewith, said spiral path of flow for the mixture of gas and solid particles and to prevent direct line flow therethrough.
  • An apparatus for pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including a plurality of nozzles angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber axially mounted as to said .vortex chamber and axially communicating therewith, said reaction chamber being constructed to provide a spiral path of flow for the mixture of gas and solid particles and to prevent direct straight line flow therethrough, and a second jacket surrounding said reaction chamber.

Description

L. BALASSA May 18, 1948.
METHOD AND APPARATUS FOR PULVERIZI ING AND PROCESSING MATERIALS Filed Jan.
ladzlslazsmaas Patented May 18, 1948 APPARATUS FOR PULVERIZ- I r I PROCESSING MATERIALS mnuunsnm, rum, Mich. Application January 4, 194:, SGIIIINO. 471,266
8 Clalml. 23-1) My invention relates to a method and apparatus for pulverizing and activating material at high temperatures,
A wide variety of pulverizing methods and apparhtus utilizing compressed air. hish pressure steam or other similar forms of fluid energy to create a vortex have been proposed and successfully employed. Such pulverizers usually consist of a circular or cylindrical vortex chamber into which the gaseous fluid is injected through one or more jets placed in such a manner as to create a vortex and to maintain the gaseous fluid in a spiralling vertex in the chamber. The material to be treated is introduced into the vortex at its periphery, and the cyclonic or tornado-like vortex of the gases sublects the entrained material to the combined effects of powerful centrifugal forces, as well as of friction and impact, both of the particles on each other and on the walls of the chamber, resulting in the reduction of the particle size of said material to a flne powder. In no case, however, did the prior art contemplate the use of fluids at high temperature, such as above 800 F., or any other change than a reduction in the particle size of the materials being treated.
My invention has as an object the utilization of high temperature. high velocity gaseous fluid for pulverizing and reacting with the material at high temperature. A further object is a method by which material suspended in a gaseous medium may be pulverized and calcined simultaneously. Another object is a method and apparatus suitable for simultaneously grinding and reducing oxide ores to metal. A further object is a method and apparatus suitable for the drying of wet mineral pigment pulps, thus avoiding th formation of hard agglomerates which necessitate further grinding. An even further object is a method and apparatus by which materials in solution may be dried in an eiilclent manner. Other objects will appear hereinafter.
In one form. these objects may be accomplished by the continuous combustion of suitable fluid fuel-air blends in a pressure combustion chamber under uniform pressure. The heat energy in the burned gases is converted into velocity by expansion, and the gases are discharged into a vortex chamber, in such a manner as to create and maintain a high velocity inwardly spiralling vortex. The gases are discharged from the center of the vortex into a reaction chamber, retaining to a large extent both their velocity and their spiral movement. The material to be treated. having a mesh size not greater than inch but verize said material.
2 preferably inch or finer is introduced into the vortex chamber where the combined eflects of the heat, high velocity, centrifugal forces, friction and impact between the particles of the material and the wall of the vortex chamber pul- The material is subjected to the physical and chemical action of the gases throughout the time of its retention in the grinding chamber and while it is passing through the reaction chamber. The chemical composition of the gases is controlled by suitable adjustments in the fuel-air ratio as well as through the introduction of other substances at any point in the vortex or reaction chamber. The eflect obtained by my methods and in my apparatus, in addition to reduction in the particle size, may be that of calcination, drying, oxidation and chemical reduction, depending on the material being treated and on the composition of the gases employed.
Referring to the drawing for a more complete disclosure of the invention,
Figure l is a vertical section of an apparatus suitable for the carrying out of my invention;
Figure 2 is a horizontal fragmentary section of the same apparatus;
Figure 3 is a diagrammatic plan view of a modified form.
The apparatus is provided with a combustion chamber I that has a heat resistant lining ii. Leading into the chamber I is a compressed air inlet pipe 2 connected to the venturi ill and leading into the mouth of the venturi is a fluid fuel inlet nozzle 3. The combustion chamber I is provided with an ignition plug 4 in one of the walls for igniting the fuel. The exit end of the chamber l is constricted to form a nozzle 5 which is connected with and tangent to the disc-shaped vortex chamber 6, the latter in turn being connected with and leading into the cylindrical reaction chamber ll of relatively smaller diameter.
The chamber II is provided on its inner'side with a spiral baifle l3 extending from the bottom to the top of chamber II, and is connected at the outlet end with the duct l2 which leads to any suitable collecting or treating apparatus.
For feeding the material to be treated into the apparatus, I provide a hopper I with an injector feeder head 9 opening into the vortex chamber 0, a compressed air or steam supply pipe 8 being connected to the feeder head.
The chambers a and ii may be provided with a water or steam jacket ls-having an intake l6 and outlet I6.
The bottom of the vortex chamber is also provided with a baflle l3a.
In the modified form shown in Fig. 3, la and lb are combustion chambers, similar to combustion chamber l of Figs. 1 and 2 in structure and arrangement. These chambers lead into the vortex chamber 6a and the products of that chamber are led from the center of the chamber 8a to the periphery of a similar central part of the vortex chamber 6b by the conduit 20. From the vortex chamber 6b, the gases are conducted through the spiral reaction chamber I lb and out the duct lib, all as in Fig. 1.
Operation Compressed air through the line 2 is forced into combustion chamber l. Fluid fuel is injected through nozzle 3. The fuel-air mixture is ignited by the glow plug 4. The diameter of nozzle is selected so that a constant pressure of approximately the same magnitude as that of the compressed air is'maintained in the combustion chamber. After the combustion chamber becomes sufiiciently hot to maintain continuous combustion, the circuit to the glow plug is broken and the fuel air-ratio is adjusted to obtain the desired effect. The high temperature products of combustion are injected, at high velocity, through nozzle 5, into the vortex chamber 6. The fluid entering tangentially, the periphery of the cylindrical vortex chamber creates a spiralling vortex and maintains it at a high rotative speed. Leaving the vortex chamber 6 through the center of the vortex, the fluid enters the reaction chamber ll. Retaining a considerable part of its rotative or spiralling motion the fluid proceeds through the reaction chamber II which is equipped with a spiral baflle l3 which aids in maintaining the rotative motion of the fluid. The material to be treated is forced through the injector feeder head 9 into the vortex chamber 6. Under the combined efi'ects of the high heat oi. the combustion gases, of the centrifugal forces created by the high velocity vortex, of the friction and impact between the particles of the material and of the walls of the vortex chamber, the material is rapidly disintegrated to a fine powder. In the vortex chamber 6 the centrifugal force keeps the larger particles near the periphery of the vortex while the smaller, finely ground particles are carried by the inwardly spiralling gaseous fluid into the reaction chamber. While being pulverized and in the reaction chamber, the material is subjected not only to the physical forces of heat, friction and impact but also to the chemical action of the gaseous fluid. Depending on the fuel-air ratio used in the combustion chamber I, the gaseous fluid exerts one of the following three eifects:
In the case of complete combustion of the fuel, with no excess oxygen present, the eflect is usuglluyd only that of the heat transmitted by the If a high fuelratio is used, leaving an excess of fuel in pa ial stages of combustion, the eifect of the fluid is strongly reducing.
With a low fuel-air ratio, resulting in a fluid containing excess oxygen, the effect will be strongly oxidizing.
After leaving the reaction chamber, the treated material, entrained in the fluid may be precipitated, either in cyclone separators utilizing the vertical energy still remaining or collected by settling in flues, by filtering with cloth,'or by magnetic or electrostatic means.
The water and steam jackets ll around the reaction and vortex chambers serve to protect the walls of the apparatus from the high heat of the gaseous fluid as well as to capture part of the waste heat. The steam produced in the jackets may be used to generate the power necessary for the operation of the process.
It will be seen that my invention is readily adaptable for the treating of materials in a variety of ways hitherto unobtainable in vortex grinding apparatus. By adjusting the fuel-air ratio in the combustion chamber I, so as to provide air in a slight excess over that theoretically required for the particular fuel used, I am able to obtain temperatures as high as 2500 F. in the vortex chamber. Under these conditions. my invention is particularly suited for the simultaneous grinding and calcination of materials. Under such conditions, I have fed a water wet mineral pigment pulp into the vortex chamber and obtained a product which was dried. finely pulverized and calcined as well.
On adjusting the fuel-air ratio to provide'an excess of fuel over that required for the oxygen present, incomplete combustion of the fuel resulted. The gases entering the vortex chamber in this case contained a high percentage of carbon monoxide, some free carbon, hydrogen and methane. The chemical effect of the gases was strongly reducing while the temperature obtained was between 1800 and 2000 F. Under these conditions I am able to reduce iron oxide ore (hematite) to metal.
With the fuel-air ratio adjusted to provide an excess of oxygen in the vortex chamber, I am able to process oxidizable materials like iron sulflde ore, simultaneously grinding and oxidizing same to iron oxide. v
In an apparatus constructed and proportioned as shown in Figs. 1 and 2, but having two combustion chambers. as shown in Fig. 3, the volume of the combustion chambers l was about 4 gallons each with nozzles 5 of A." diameter, the vortex chamber 6 had a diameter of 38" and a height of 5 3" measured from inside to inside of the base plate and the top at the periphery of the vortex chamber. The reaction chamber l I had an inside diameter of 24" and a height of ten feet. The injector feeder head 9 had a nozzle with a opening and the venturi opening of A" in diameter at its narrowest part.
The following examples describe operating conditions under which satisfactory results have been obtained in accordance with my invention.
Example 1 Air at a pressure of 40 lbs. per square inch'was I introduced into the combustion chamber. Fuel oil was introduced at first in sufiicient amount to obtain complete combustion. After the combustion chamber became sufficiently hot to support combustion, the fuel-air ratio was adjusted to the Example 2 Using air at a pressure of 40 lbs. per square inch and only the minimum of fuel, with which continuous combustion could be maintained, a gaseous fiuid with highly oxidizing character was obtained. When coarse iron sulfide ore (pyrites) was introduced into the vortex chamber. iron oxide having an average particle size of two microns was collected in the fines.
Example 3 Example 4 The conditions of Example 3 were maintained in this experiment. When a 50% solution of ferric sulfate (coquimbite) in water was fed into the vortex chamber, finely pulverized iron oxide was recovered from the centrifugal separator.
Example 5 The conditions of Example 3 were maintained in this experiment, but the apparatus was changed to have the vortex chamber'l in vertical position, and the reaction chamber I I in horizontal position. When a mixture of 2 mols of sodium carbonate and one mol of silica was fed into the vortex chamber, fused sodium meta-silicate was obtained from the centrifugal separator.
Example 6 The conditions of Example 3 were maintained in this experiment. When a water wet pulp of acid treated barium sulfate containing 30% water was fed into the vortex chamber, a highly calcined and finely pulverized product of good white color was obtained.
Example 7 The conditions of Example 5 were maintained in this experiment, using hydrogen as fuel. When a 25% solution of sodium hydroxide in water was fed into the vortex chamber, fused sodium hydroxide of around 90% NaOH content was obtained from the centrifugal separator.
Example 8 The conditions of Example 3 were maintained in this experiment. When a mixture of calcium carbonate and silica in equi-molecular proportions was fed into the vortex chamber finely pulverized calcium silicate was obtained from the centrifugal separator.
It is apparent that a great many variations of the above apparatus as to dimensions, types of feeding, etc., are possible within the principles laid down by my invention. The apparatus if desired may be constructed of metal or of suitable ceramic materials, The combustion chambers may be of any suitable design or shape and are preferably lined with fire brick. The nozzle 0 should preferably be of quartz or other similar heat resisting material. The glow plug 4 may be of any of the standard designs used in Diesel engines or it may be substituted by a spark plug or glow wire. In the preferred embodiment of my invention. I have utilized the gaseous fluid obtained through continuous combustion of a fuel-air mixture under pressure. Satisfactory results may be obtained, however, also if the fluid is produced through intermittent combustion or through successive explosions of the fuel-air mixture and irrespective of whether the fuel-air mixture was compressed before ignition or if it was ignited at atmospheric pressure.
While I have disclosed as a preferred embodiment, the use of a fluid fuel-air combustible mixture, other combinations of gases, liquids and solids are within the scope of my invention, where they combine with an exothermic reaction and where the products of the reaction are I have a substantially greater volume at the same pressure than the volume introduced intdthe vortex chamber, thus producing increased velocity in the vortex chamber.
Any of the conventional combustible fuels meeting the above requirements may be employed, such as furnace oil, Diesel oil, kerosene, illuminating, natural and water gas, hydrogen. butane and the like and powdered coal.
The operating pressure in the combustion chamber may range from 30 lbs. per square inch up, depending on the construction of the apparatus. In the type of apparatus disclosed in Figs. 1 and 2. the pressure in the vortex and reaction chambers will usually be near atmospheric but it may reach substantially higher pressures. High pressures are used when the vortex chambers are hooked up in tandem, as shown in Fig. 3, for the gradual stepwise expansion of the gases.
The most useful range of operating temperatures will lie between 1000-1800 C. in the combustion chamber, and between 800-1400 C. in the vortex and reaction chambers, although high temperatures are operative in both chambers.
The speed of the vortex is above 20,000 R. P. M. and preferably about 40,000 R. P. M.
While I prefer to have the vortex chamber in horizontal position. with the reaction chamber in vertical position, the reversal of the relative position of the two chambers does not materially affect the functioning of my apparatus and is within the scope of my invention.
In order to extend the processing time of materials that are difficult to oxidize or reduce, the
reaction chamber may be lengthened to any extent necessary to obtain a retention time sumcient for the completion of the reaction in question. Both the vortex and the reaction chamber may be equipped with jets suitable for the iniectlon of air, steam or other gases to modify the quality a of the product obtained.
By coupling two or more vortex chambers, as shown in Fig. 3, in such a manner as to force the fluid leaving the center of the first vortex chamber into the rim of the second and repeating this process any desired number of times until the pressure of the gases drops to atmosphere pressure, it is possible to provide a step-wise expansion of the combustion gases generated in the combustion chamber. At any desired stage of this process the volume velocity or composition of the gases may be increased or otherwise changed through the introduction of gases generated in additional combustion chambers.
If desired, the direction of the reaction may be changed from oxidation to reduction or vice versa by changing the composition of the gases at various stages. For instance, calcining in the first stage with a slight excess of air and then in the second stage introducing a reducing gas like methane or ethyl alcohol, which after exhausting the excess oxygen provides a strong reducing atmosphere.
gases-that.
My invention has the following advantages over the prior art:
1. It provides for a more eillcient use oiiluid energy. I obtain about the same grinding effect with a compressed air supply of 40 lbs. pressure to the fuel-air blend, as the prior art would obtain at around 250 lbs. pressure with air alone. This is due to the increased volume or the gases oi combustion at the high operating temperature of my apparatus. 2. It utilizes high heat gaseous vortex io'r pulverizing and for effecting simultaneously one or more physical and chemical processes at temperatures beyond the reach or prior art.
3. It provides the conditions which make it possible to pulverize materials and simultaneously effect physical and chemical changes such as calcination, oxidation, reduction and chemical combination of two or more materials.
4. It makes it possible to control the composition and the temperature of the gaseous fluid during the process, through changes in the fuelair ratio or through introduction of air, steam or other fluid at any desired stage of the process or by increasing the circulation of the liquid in the jackets. In other words, when the hot gases of combustion flow through the nozzle into the grinding chamber 6, applicant derives the same benefit from the drop in pressure from that in the combustion chamber to a pressure only slightly above atmospheric which exists in the grinding chamber that is realized in the prior art, but, in addition, the drop in temperature converts alarge proportion oi the heat in the gases into kinetic .energy, which is expended in increasing the velocity of the gases in the grinding chamber.
It will be seen from the above examples that there may be provided procedures and methods of construction which vary considerably but which yet embody the iundamental and novel concepts of my invention.
Since certain changes in the construction or my apparatus and in carrying out my processes, which embody the invention, may be made without departing from its scope. it is intended that all matter contained in the above description or shown in the accompanying drawing shall serve merely as illustration and not limiting in any sense. 5
I claim:
1. A method of pulverlzing solid material and simultaneously chemically reacting said material at high temperatures comprising the steps of leading a combustible mixture into a combustion chamber and burning the same under conditions which create high temperatures and pressures in said chamber, leading the combustion gases from said combustion chamber through a narrow passageway to a circular vortex chamber and introducing the combustion gases from said passageway tangentially into said circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, simultaneously cooling the vortex chamber and introducing the gases into a reaction chamber which conducts the material and gases through a prolonged path in the reaction chamber whereby slowing down of the gases is effected and causes substantial completion of said reaction.
2. A method of pulverizing solid material and simultaneously chemically reacting said material -said combustion chamber through a narrow passageway to a circular vortex chamber and introducing the combustion gases from said passageway tangentially into said circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, introducing the gases into a reaction chamber which conducts the material and gases through a prolonged path in the reaction chamber whereby slowing down of the gases is effected and causes substantial completion of said reaction, and simultaneously cool- };g the vortex chamber and the reaction cham- 3. A method of pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising the steps of leading a-combustible mixture into a combustion chamber and burning the same under conditions which create high temperatures and pressures in said chamber, leading the combustion gases from said combustion chamber through a narrow passageway to a-circular vortex chamber and introducing the combustion gases from said passageway tangentially into said circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, simultaneously cooling the vortex chamber and introducing the gases into a reaction chamber which conducts the material and gases through a spiral path in the reaction chamber whereby slowing down of the gases is eflected and causes substantial completion of said reaction.
- 4. A method of pulverizing solid material and simultaneously chemically reacting said material at high temperatures comprising the steps of leading a combustible mixture into a combustion chamber and burning the same under conditions which create high temperatures and pressures in said chamber, leading the combustion gases from said combustion chamber through a narrow passageway while simultaneously cooling said passageway at a point adjacent to its connection to said vortex chamber and introducing the combustion gases from said passageway tangentially into a circular vortex chamber at high temperatures and pressures, the gases moving at high speeds spirally in said vortex chamber, while concurrently introducing solid material to be processed into said gases in said vortex chamber at a pressure in excess of the pressure in said vortex chamber, simultaneously cooling the vortex chamber and introducing the gases into a reaction chamber which conducts the material. and gases through a prolonged path in the reaction chamber whereby slowing down 01' the gases is eflected and causes substantial completion of said reaction.
5. An apparatus for puiverizing solid material and simultaneously chemically reacting said material at high temperatures, comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including at least one nozzle angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to. its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber axially mounted as to said vortex chamber and axially communicating therewith, said reaction chamber being constructed to provide an elongated path of flow for the mixture of gas and solid particles and to prevent direct straight line flow therethrough.
6. An'apparatus for pulverizing solid material and simultaneously chemically reacting said material at high temperatures, comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including at least one nozzle angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber, means mounting said reaction chamber above and axially aligned as to said vortex chamber and axially communicating therewith, said reaction chamber being constructed to provide an elongated path of flow for the mixture of gas and solid particles and to prevent direct straight line flow therethrough.
7. An apparatus for pulverizing solid material and simultaneously chemically reacting said material at high temperatures, comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including at least one nozzle angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber axially mounted as to said vortex chamreaction chamber being constructed to provide a 10 ber and axially communicating therewith, said spiral path of flow for the mixture of gas and solid particles and to prevent direct line flow therethrough.
8. An apparatus for pulverizing solid material and simultaneously chemically reacting said material at high temperatures, comprising a combustion chamber, a relatively shallow circular vortex chamber, means connecting the combustion chamber with the vortex chamber including a plurality of nozzles angularly connected to the periphery of the vortex chamber, a fuel inlet for said combustion chamber, ignition means in said combustion chamber, an inlet into said vortex chamber in proximity to its circumference for the admission of solid comminuted material, a jacket surrounding said vortex chamber, a reaction chamber axially mounted as to said .vortex chamber and axially communicating therewith, said reaction chamber being constructed to provide a spiral path of flow for the mixture of gas and solid particles and to prevent direct straight line flow therethrough, and a second jacket surrounding said reaction chamber.
LADISLAUS BALASSA.
REFERENCES CITED The following references are of record in the file of this patent:
UNITED STATES PATENTS Number Name Date 729,008 Sutton May 26, 1903 129,009 Sutton et al May 26, 1903 Re. 12,424 Brown Dec. 12, 1905 1,328,446 Odam Jan. 20, 1920 1,840,857 Testrup Jan. 12, 1932 2,032,827 Andrews Mar. 3, 1936 2,055,385 Noack Sept. 22, 1936 2,163,762 Noack June 2'7, 1939 2,184,300 Hudson ct a1. Dec. 26, 1939 2,257,907 Griswold Oct. 7, 1941 2,306,462 Moorman Dec. 29, 1942 FOREIGN PATENTS Number Country Date 7 469,068 Great Britain July 19, 1937
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Cited By (23)

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US2600837A (en) * 1947-08-06 1952-06-17 Clay G Boyer Device for removing wrappers from packaged goods, such as chewing gum, confections, or the like
US2707594A (en) * 1951-08-06 1955-05-03 Jack K Moore Method and apparatus for reducing materials
US2728995A (en) * 1951-08-04 1956-01-03 Ruhrchemie Ag Drying granular material
US2743289A (en) * 1951-05-30 1956-04-24 Stamicarbon Process of effecting exothermal chemical reactions between difficultly miscible liquids
US2752097A (en) * 1951-03-03 1956-06-26 Microcyclomat Co Method and apparatus for the production of fine and ultrafine particles
US2826369A (en) * 1952-02-19 1958-03-11 Bayer Ag Comminution by successive explosions
US2830769A (en) * 1953-05-18 1958-04-15 Texaco Development Corp Method and apparatus for treating a solid material
US2865820A (en) * 1951-04-18 1958-12-23 Koppers Co Inc Method for heat treatment of finely divided solid media
US2890929A (en) * 1954-12-31 1959-06-16 Hoechst Ag Process for carrying out exothermic chemical reactions
DE973676C (en) * 1951-08-05 1960-04-28 Ruhrchemie Ag Dryer for waste materials
US2942043A (en) * 1955-01-03 1960-06-21 Hoechst Ag Process for carrying out endothermic chemical reactions
US2954303A (en) * 1956-04-17 1960-09-27 American Pigment Corp Production of ferromagnetic oxide
US2984544A (en) * 1956-04-05 1961-05-16 Comp Generale Electricite Process for the preparation of lead oxide
US2985506A (en) * 1957-12-06 1961-05-23 Vita Sam Di Method of producing barium titanate
US3021195A (en) * 1958-01-02 1962-02-13 Bayer Ag Treatment of silicates
US3136536A (en) * 1960-08-12 1964-06-09 Allis Chalmers Mfg Co Treating finely divided material in suspension
US3140862A (en) * 1958-10-06 1964-07-14 Metallbau Semler G M B H Apparatus for the physical and/or chemical treatment of granular solids or fine dusts
US3200512A (en) * 1962-01-05 1965-08-17 Augustine J Tucker Apparatus for gas-jet propelling and heating granular material
US3485487A (en) * 1967-01-10 1969-12-23 Litton Precision Prod Inc Method and apparatus for beneficiating ores
US3580552A (en) * 1968-04-24 1971-05-25 Smidth & Co As F L Stack preheater
US3612143A (en) * 1969-11-03 1971-10-12 Standard Products Co Apparatus for liquid waste disposal
US3802089A (en) * 1973-04-02 1974-04-09 Fluid Energy Process Equip Method and apparatus for treating waste products
US4056233A (en) * 1976-10-01 1977-11-01 Fay Edwin F Apparatus for pulverizing solid materials

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US1328446A (en) * 1919-01-02 1920-01-20 Odam Eugene Process and apparatus for atomizing materials in a melted state
US1840857A (en) * 1928-03-01 1932-01-12 Techno Chemical Lab Ltd Drying device
US2055385A (en) * 1933-08-08 1936-09-22 Bbc Brown Boveri & Cie Pulverizing plant
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Cited By (23)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2600837A (en) * 1947-08-06 1952-06-17 Clay G Boyer Device for removing wrappers from packaged goods, such as chewing gum, confections, or the like
US2752097A (en) * 1951-03-03 1956-06-26 Microcyclomat Co Method and apparatus for the production of fine and ultrafine particles
US2865820A (en) * 1951-04-18 1958-12-23 Koppers Co Inc Method for heat treatment of finely divided solid media
US2743289A (en) * 1951-05-30 1956-04-24 Stamicarbon Process of effecting exothermal chemical reactions between difficultly miscible liquids
US2728995A (en) * 1951-08-04 1956-01-03 Ruhrchemie Ag Drying granular material
DE973676C (en) * 1951-08-05 1960-04-28 Ruhrchemie Ag Dryer for waste materials
US2707594A (en) * 1951-08-06 1955-05-03 Jack K Moore Method and apparatus for reducing materials
US2826369A (en) * 1952-02-19 1958-03-11 Bayer Ag Comminution by successive explosions
US2830769A (en) * 1953-05-18 1958-04-15 Texaco Development Corp Method and apparatus for treating a solid material
US2890929A (en) * 1954-12-31 1959-06-16 Hoechst Ag Process for carrying out exothermic chemical reactions
US2942043A (en) * 1955-01-03 1960-06-21 Hoechst Ag Process for carrying out endothermic chemical reactions
US2984544A (en) * 1956-04-05 1961-05-16 Comp Generale Electricite Process for the preparation of lead oxide
US2954303A (en) * 1956-04-17 1960-09-27 American Pigment Corp Production of ferromagnetic oxide
US2985506A (en) * 1957-12-06 1961-05-23 Vita Sam Di Method of producing barium titanate
US3021195A (en) * 1958-01-02 1962-02-13 Bayer Ag Treatment of silicates
US3140862A (en) * 1958-10-06 1964-07-14 Metallbau Semler G M B H Apparatus for the physical and/or chemical treatment of granular solids or fine dusts
US3136536A (en) * 1960-08-12 1964-06-09 Allis Chalmers Mfg Co Treating finely divided material in suspension
US3200512A (en) * 1962-01-05 1965-08-17 Augustine J Tucker Apparatus for gas-jet propelling and heating granular material
US3485487A (en) * 1967-01-10 1969-12-23 Litton Precision Prod Inc Method and apparatus for beneficiating ores
US3580552A (en) * 1968-04-24 1971-05-25 Smidth & Co As F L Stack preheater
US3612143A (en) * 1969-11-03 1971-10-12 Standard Products Co Apparatus for liquid waste disposal
US3802089A (en) * 1973-04-02 1974-04-09 Fluid Energy Process Equip Method and apparatus for treating waste products
US4056233A (en) * 1976-10-01 1977-11-01 Fay Edwin F Apparatus for pulverizing solid materials

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