US3493182A - Grinding and apparatus therefor - Google Patents

Grinding and apparatus therefor Download PDF

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Publication number
US3493182A
US3493182A US591459A US3493182DA US3493182A US 3493182 A US3493182 A US 3493182A US 591459 A US591459 A US 591459A US 3493182D A US3493182D A US 3493182DA US 3493182 A US3493182 A US 3493182A
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grinding
grinding media
continuous
media
diminution
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Andrew Szegvari
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UNION PROCESS INTERNATIONAL Inc AN OH CORP
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Individual
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Assigned to UNION PROCESS INTERNATIONAL, INC. AN OH CORP. reassignment UNION PROCESS INTERNATIONAL, INC. AN OH CORP. ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: ARNO, SZEGVARI, ADMINISTRATOR, DBN/WWA OF THE ESTATE OF ANDREW SZEGVARI, DEC`D
Assigned to SZEGVARI, ARNO ADMINISTRATOR DE BONIS NON OF THE ESTATE OF ANDREW SZEGVARI, DEC'D. reassignment SZEGVARI, ARNO ADMINISTRATOR DE BONIS NON OF THE ESTATE OF ANDREW SZEGVARI, DEC'D. LETTERS OF ADMINISTRATION (SEE DOCUMENT FOR DETAILS). EFFECTIVE MARCH 27, 1981. Assignors: SZEGVARI, ANDREW, DEC'D.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
    • B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
    • B02C17/00—Disintegrating by tumbling mills, i.e. mills having a container charged with the material to be disintegrated with or without special disintegrating members such as pebbles or balls
    • B02C17/16—Mills in which a fixed container houses stirring means tumbling the charge

Definitions

  • Elimination of the largest or coarsest particles That is reduction of the area of the distribution curve under the large end and in addition terminating it (FIGURE 2), or bringing it to practically zero at the required size. This can be most effectively done with large or larger grinding media and in a batch type operation easier than in a continuous operation.
  • the invention relates to fine grinding-the grinding of pumpable dispersions which is quite different from coarse grinding. Fine grinding is applied to pigments for paints and inks, drugs, ferrites, etc. The industrial purposes and controlling factors of ne grinding are entirely different from those of coarse grinding. The only purpose of coarse grinding is diminution. The purpose of ⁇ fine grinding is to obtain certain definite and sensitive properties of the end product not otherwise obtainable. These are reflected in the distribution curve.
  • FIGURE 2 is a family of graphs, with the vertical axis measuring pre-mixing time in minutes required to arrive at a certain Hegman neness (using activated grinding media), and the horizontal axis indicating the grindability of the particular slurry in some practical units thus indicating the grindability of the particular dispersion in a practical yardstick.
  • the ordinarily well-known grinding time in conventional ball mills expressed in hours.
  • FIGURE 3 is a ow sheet of various processing operations which are within the scope of the invention.
  • FIGURE 4 is a representation, largely schematic, of apparatus for carrying out Process D of FIGURE 3;
  • FIGURE 5 is a representation, largely schematic, of apparatus for carrying out Process E of FIGURE 3.
  • FIGURES 6a to 6d are distribution curves.
  • FIGURE 6a is a representative distribution curve of the particle sizes of a solid powder.
  • FIGURE 6b shows in dotted lines the effect oif diminution using relatively large grinding media (the solid line showing is the original FIGURE 6a).
  • FIGURE 6c shows in solid lines the effect of diminution with relatively small grinding media, the solid line showing is the original curve of FIGURE 6a.
  • FIGURE 6d shows the curve of FIGURE 6a to the right, and to the left shows the effect of a batch and a continuous operation carried out to the same particle size.
  • FIGURE l shows the iineness expressed in Hegman gauge grades, as a grinding progresses, which applies generally to the effect of activated grinding media on solids in liquids.
  • the horizontal axis is scaled so as to indicate full grinding time of 100, regardless of how long the grinding continues. This applies to all materials and equipment.
  • the percentage means simply the percentage of the ⁇ full grinding time expressed in the same time scale.
  • the graph shows the extremely rapid rise in the amount of fine particles obtained during the rst few percent of the elapsed total grinding time.
  • FIGURE 2 indicates that when pre-mixing in a batch type pre-mixer, containing activated grinding media such as described for use in Process D below, one can obtain 3 to 5 Hegman grade fineness in a relatively few minutes, mostly less than 10 minutes, with any slurry with usual average grindability, such as finished in a conventional ball mill within two days.
  • Process A This is a general process illustrated schematically, in which any two types of grinding equipment containing activated grinding media are used with the grinding media in the first vessel or larger size than those in the second vessel.
  • the suspension produced in the first vessel is conveyed continuously or intermittently to the second vessel.
  • Process A The processes following Process A are selected as presently appearing to have the greatest commercial possibilities.
  • Processes C and D are particularly adapted for use in the ne grinding of pigments for paints, inks, etc., and other processes may be particularly adapted lfor the grinding of other solids including drugs and inorganic materials.
  • Process B Process using a pre-mixing device containing activated grinding media which discharges into continuous grinding equipment, with or without an intermediate converter.
  • Process D Solid and liquid components of a slurry are combined conventionally and fed into a pre-grinding device containing activated grinding media and by way of the instrumentality of a converting mechanism feeding into a continuously grinding unit.
  • An example for this process is the large-scale production of the so-called white base of the paint industry consisting essentially of a titanium dioxide pigment suspended in the properly formulated slurry.
  • the pigment which may be of a size of about 325 mesh, will, for example, be fed once a day with the suspending medium to a premixer 1 which may be a 60G-gallon tank.
  • These pre-grinders may each have a capacity of about 40 gallons and will grind the pigment to an average Hegman gauge of 4 to 5.
  • the finished pre-mix is metered automatically and continuously by way of the controlling monitor 3- and pump 6 into the continuous grinding unit 7 which contains grinding media in the size range between 1&4 to M3 inch.
  • This unit 7 may be of the type illustrated and described in Szegvari U.S. 3,149,789.
  • the solids are ground to an average Hegman fneness greater than 7.
  • Process E The solid and liquid components of the slurry are charged into the pre-mixer 10' containing activated grinding media, and pumped intermittently by pump 11 into an intermediate pre-mix accumulator 12.
  • the size of this accumulator is such that it can provide continuous feeding through a metering pump 13 to the continuous grinding device 14, requiring at least two over-lapping periods of the pre-mixer 10.
  • the device 14 may be of the type described in Szegvari U.S. 3,149,789.
  • the pre-mixer 10 may be, 4for example, ⁇ of Al0-gallon capacity, and using balls Vs inch in diameter will produce a pre-mix of a size of about Hegman gauge 21/2 to 41/2 every ⁇ 10 minutes.
  • smaller grinding media will be used in the range of %4 inch to s inch and the processed slurry will be ground to a Hegman gauge of 71/2 to 8.
  • Process F Sluriy pre-mixed in any type of pre-mixing device is metered into a continuous grinding device from which a product issues into a second continuous grinding device.
  • These continuous grinding devices contain grinding media in the range between 1/s inch and 1764 inch; the rst grinding device having grinding media in the range between 1A; inch and 3,32 inch and the second continuous grinding device having grinding media in the range between 3/32 inch and 1/16 inch.
  • the first and second grinding devices may have additional differences, namely, the r.p.m. of the first grinding device may be between the range of 100 and 600 r.p.m., while in the second grinding device, the r.p.m. may be in the range between 150 and 1000 r.p.m.
  • Apparatus such as described in Szegvari U.S. 3,149,789 may be used for for each of these continuous grinding units. This process is adapted for the fine grinding of powders, drugs, etc. to an average particle size in the range of 1 to 2 microns.
  • this pre-mixer resembles the grinding device disclosed in Sztgvari U.S. 2,764,359 but generally it will not contain as many grinding media as used in a commercial grinding operation.
  • the grinding media will usually -by of a size of at least between M1 inch and 3A; inch.
  • the top of the tank will conveniently be equipped with an apron to facilitate manual loading with solid and liquid feed material and it will be equipped with a discharge conduit suitable for continuous or intermittent discharge of the slurry to a ow converter or a continuous grinder or other equipment as required.
  • Discharge opening is provided for the discharge of the pre-mixed slurry and the grinding media. Exposed parts of the drive are protected from contamination by ingredients floating in the air as a result of the loading process. All apparatus details which serve the purpose of finishing the grinding to ultimate iineness, such as cooling means and specific tank handling equipment are omitted.
  • a converter is used for the purpose of changing intermittent discharge from the premixing devices containing activated grinding media into a continuous iiow to feed continuous grinding apparatus.
  • FIGURE 5 indicates the use of an intermediate premix flow-converter, the regulation of which is manually controlled, following the preferred type of pre-mixer, an Attritor pre-mixer, just described.
  • FIGURE 4 shows an apparatus where a large quantity of solid and liquid, for instance, the entire supply used in one shift, is combined in a container of suicient size; the size of the container might be -between 200 and 800 ⁇ gallons.
  • These containers are equipped with a conventional agitator to assist in the distribution of solids in the liquids and to keep the distributed solids from excessive sedimentation. No grinding media are used.
  • the control of the flow which involves charging the twin pre-mixers containing activated grinding media, and the subsequent intermittent discharging of each of these pre-mixers into the continuous grinding equipment, is controlled by an electric monitoring device which acts on the four valves to control the intermittent charging and the discharging of the twin system.
  • the controls of the monitor are effected by conventional timing apparatus to control the iineness to which the particles are ground in the :separate grinding operations and thus make the process selective and conventional level control apparatus.

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  • Engineering & Computer Science (AREA)
  • Food Science & Technology (AREA)
  • Crushing And Grinding (AREA)
  • Grinding-Machine Dressing And Accessory Apparatuses (AREA)
US591459A 1966-11-02 1966-11-02 Grinding and apparatus therefor Expired - Lifetime US3493182A (en)

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US59145966A 1966-11-02 1966-11-02

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US (1) US3493182A (de)
AT (1) AT307213B (de)
CH (1) CH516347A (de)
GB (1) GB1208887A (de)
NL (1) NL6714905A (de)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3628739A (en) * 1968-10-03 1971-12-21 Knapsack Ag Process for the manufacture of most finely pulverized red phosphorus
US3645456A (en) * 1968-06-05 1972-02-29 Mo Och Domsjoe Ab Method for converting sheet cellulose pulp to defibrated pulp
US6043175A (en) * 1992-12-08 2000-03-28 Vkvs Worldwide Corporation Method and apparatus for producing a silicon based binding composition and product prepared therefrom

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US241653A (en) * 1881-05-17 Drying apparatus
US569828A (en) * 1896-10-20 Albert herzfeld
US1361205A (en) * 1916-10-02 1920-12-07 Allis Chalmers Mfg Co Combination mill and process of efficient operation thereof
US1951823A (en) * 1930-04-07 1934-03-20 Walter P Eppers Grinding mill
US2168086A (en) * 1934-12-31 1939-08-01 Sullivan Machinery Co Mill
US2719009A (en) * 1954-08-12 1955-09-27 Clevite Corp Method of producing an elastomer dispersible magnetic iron oxide
US2764359A (en) * 1950-05-24 1956-09-25 Szegvari Andrew Treatment of liquid systems and apparatus therefor
US3210239A (en) * 1962-06-21 1965-10-05 Scott Paper Co Process of forming paper containing foamed aminoplast resins
US3275250A (en) * 1963-10-14 1966-09-27 Hercules Inc Process for making fine particles of nitrocellulose

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US241653A (en) * 1881-05-17 Drying apparatus
US569828A (en) * 1896-10-20 Albert herzfeld
US1361205A (en) * 1916-10-02 1920-12-07 Allis Chalmers Mfg Co Combination mill and process of efficient operation thereof
US1951823A (en) * 1930-04-07 1934-03-20 Walter P Eppers Grinding mill
US2168086A (en) * 1934-12-31 1939-08-01 Sullivan Machinery Co Mill
US2764359A (en) * 1950-05-24 1956-09-25 Szegvari Andrew Treatment of liquid systems and apparatus therefor
US2719009A (en) * 1954-08-12 1955-09-27 Clevite Corp Method of producing an elastomer dispersible magnetic iron oxide
US3210239A (en) * 1962-06-21 1965-10-05 Scott Paper Co Process of forming paper containing foamed aminoplast resins
US3275250A (en) * 1963-10-14 1966-09-27 Hercules Inc Process for making fine particles of nitrocellulose

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3645456A (en) * 1968-06-05 1972-02-29 Mo Och Domsjoe Ab Method for converting sheet cellulose pulp to defibrated pulp
US3628739A (en) * 1968-10-03 1971-12-21 Knapsack Ag Process for the manufacture of most finely pulverized red phosphorus
US6043175A (en) * 1992-12-08 2000-03-28 Vkvs Worldwide Corporation Method and apparatus for producing a silicon based binding composition and product prepared therefrom

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Publication number Publication date
GB1208887A (en) 1970-10-14
AT307213B (de) 1973-05-10
CH516347A (de) 1971-12-15
NL6714905A (de) 1968-05-03

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AS Assignment

Owner name: UNION PROCESS INTERNATIONAL, INC. 1925 AKRON-PENIN

Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:ARNO, SZEGVARI, ADMINISTRATOR, DBN/WWA OF THE ESTATE OF ANDREW SZEGVARI, DEC`D;REEL/FRAME:004303/0006

Effective date: 19840306

AS Assignment

Owner name: SZEGVARI, ARNO ADMINISTRATOR DE BONIS NON OF THE E

Free format text: LETTERS OF ADMINISTRATION;ASSIGNOR:SZEGVARI, ANDREW, DEC D.;REEL/FRAME:004300/0101

Effective date: 19840628