US3262213A - Method and apparatus for drying agglomerates - Google Patents

Method and apparatus for drying agglomerates Download PDF

Info

Publication number
US3262213A
US3262213A US270069A US27006963A US3262213A US 3262213 A US3262213 A US 3262213A US 270069 A US270069 A US 270069A US 27006963 A US27006963 A US 27006963A US 3262213 A US3262213 A US 3262213A
Authority
US
United States
Prior art keywords
agglomerates
drying
air
moist
chamber
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Expired - Lifetime
Application number
US270069A
Other languages
English (en)
Inventor
Curtis L Austin
Donald E Schaetzel
Riconda Leo
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
General Mills Inc
Original Assignee
General Mills Inc
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Application filed by General Mills Inc filed Critical General Mills Inc
Priority to US270069A priority Critical patent/US3262213A/en
Priority to GB51428/63A priority patent/GB1069838A/en
Priority to SE347/64A priority patent/SE319140B/xx
Priority to CH29164A priority patent/CH418980A/de
Application granted granted Critical
Publication of US3262213A publication Critical patent/US3262213A/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Images

Classifications

    • 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
    • F26B17/101—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 the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis
    • F26B17/103—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 the drying enclosure having the shape of one or a plurality of shafts or ducts, e.g. with substantially straight and vertical axis with specific material feeding arrangements, e.g. combined with disintegrating means
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23P—SHAPING OR WORKING OF FOODSTUFFS, NOT FULLY COVERED BY A SINGLE OTHER SUBCLASS
    • A23P10/00—Shaping or working of foodstuffs characterised by the products
    • A23P10/20—Agglomerating; Granulating; Tabletting
    • 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

Definitions

  • Certain objects of the present invention are accomplished by a process of drying fragile, moist agglomerates which may involve feeding the agglomerates to a drying zone wherein air or gas moves uninterruptedly and vertically downward throughout the entire drying zone, introducing the agglomerates into a drying gas or air stream entering the top of the drying zone, co-currently passing the drying gas and agglomerates downward through the drying zone, and recovering dried agglomerates from the drying zone.
  • a drying and separating apparatus which may include, among other things, a vertical tubular drying chamber in which heated gas or air from a heater is introduced into the top of the chamber together with moist agglomerates.
  • a separating device is located at the foot or exit of the drying chamber to separate the dried agglomerates from the heated gas or air.
  • the process and the apparatus for carrying out the process provides a unique and highly effective method and apparatus for drying moist agglomerates.
  • the agglomerates are able to pass through the system and be dried with a minimum of agitation and impaction. Indeed, they fall freely throughout the entire drying operation and therefore damage to the product is virtually nonexistent.
  • FIGURE 1 is a front schematic diagram illustrating a preferred drying system and apparatu used in the present invention
  • FIGURE 2 is a fractional, partially in section of the upper end of the device of FIGURE 1 showing details of the drying system and apparatus where the air and moist agglomerated particles are mixed,
  • FIGURE 3 is an isometric view of a portion of the device of FIGURE 2,
  • FIGURE 4 is a sectional view taken generally along and in the direction of lines 4-4 of FIGURE 1, and
  • FIGURE 5 is a fractional isometric view of a section of a cone shown in FIGURE 2.
  • FIGURES 1 and 2 illustrate certain preferred embodiments of the present invention.
  • the invention concerns drying fragile, moist agglomerates which are passed through a drying zone co-currently with a drying gas or air. Individual particles of material to be agglomerated are formed into small moist agglomerates 12 in the agglomerator 10.
  • the agglomerator operates by moistening the particles with water or a similar agglomerating fluid while contacting the particles with one another so that agglomerates are formed.
  • suitable devices and methods are known in the art for accomplishing this result.
  • the moist agglomerates 12 are introduced from the agglomerator into the receiving tube 17. Instead of feeding the moist agglomerates directly as is illustrated, one may also feed the agglomerates to the receiving tube 17 by means of a conveyor belt or some other suitable device. Because of the fragile and sticky nature of the agglomerates it is desirable to feed them directly from the agglomerator into the receiving tube.
  • the moist agglomerates 12 pass from the receiving tube into the inner portion of the air inlet cone 18. Heated air 11 from the air heater 13 flows through the air duct 14 into the plenum chamber 15. The hot air 11 flows through the perforations 20 of the air inlet cone 18 in a downward direction and engages and intimately mixes with the moist agglomerates 12 and carries them intothe drying chamber 21.
  • the design of the air inlet cone 18 depends a great deal upon the method of feeding the agglomerates 12 into the drying system. Where the agglomerator 10 is mounted directly above the drying chamber 21 so that the particles enter the drying chamber 21 with considerable velocity, the air inlet cone 18 is desirable.
  • the openings in the cone should be at such an angle and of such size to prevent moist agglomerates 12 from sticking to the sides of the air inlet cone 18, or passing through the perforations 20 of the air inlet cone 18 and becoming lodged between the cone and the wall of the drying chamber 21.
  • the openings or perforations 20 are uniformly spaced over the entire surface of cone 18 so that the air enters the cone uniformly from all sides to direct the particles away from the sides of the cone 18.
  • the perforations 20 are provided with baflles or cut at a suitable angle into the wall of cone 18 (see FIG. 5) so that a particle 12 which is moving toward the wall of the cone 18 will be deflected by hot gas or air 11 entering the cone 18 from duct 14.
  • the entrance angle of the air 11 will depend on the direction of flow of the particles 12, the velocity of the particles, the slope of the walls of the cone 18 and the velocity of the air 11. These factors are controlled so that the laminar flow of the hot air and particles 12' does not result.
  • True laminar flow reduces the efliciency of the drying.
  • air velocities of 3,000 to 5,000 feet per minute are sufficient in most instances to prevent sticking, escape of the agglomerates and efiicient drying.
  • the optimum air fiow rate will necessarily depend upon the force with which the moist agglomerates 12 are introduced into the drying chamber 21.
  • the drying chamber 21 is a generally vertical tube, preferably of circular cross-section, which is free of baffles and other interruptions so that a free, uninterrupted flow of air is obtained. If the drying chamber contains interruptions, there will be undesirable agitation and moist agglomerates will be further agglomerated to an undesirably large size or broken down into undesirably small particles.
  • the heated air 11 flows downward in the drying chamber 21 at a speed of about 500-4,000 feet per minute and preferably about LOGO-2,000 feet per minute, while the agglomerates move at a somewhat different velocity due to the additional influence, for example, gravity acting on the aglomerates.
  • the agglomerates might be accelerated above the air velocity by other well known means to attain the velocity differential. It is advantageous to employ as low an air speed as is practical to avoid damaging the particles. High air velocities cause breakage of the agglomerates during drying and low air velocities are not conductive to good drying.
  • the drying chamber 21 should have a length generally in the range of 200 feet and preferably in the range of 25-100 feet.
  • the temperature of the heated air 11 decreases throughout the length of the drier in proportion to the amount of drying.
  • the heated air 11 enters the drying chamber 21 at temperatures of up to about 400 F. and preferably from about 250-300 F.
  • the optimum temperature depends upon the moisture content of the moist agglomerates 12, moisture content of the incoming air, the size of the agglomerates, upon the time of travel through the drying chamber 21 and the ratio of solids to
  • the drier exit stream 24 leaves the drying chamber 21 and enters the separation chamber 25.
  • the air temperature is about 100-200" F. and preferably about 150 F. More desirably, the temperature is as close to the product temperature as possible.
  • the product temperature for a typical flour product would be about 120 F.
  • the separation chamber 25 is of greatly enlarged cross section as compared to the cross section of the drying chamber 21.
  • the decreased air velocity in the separation chamber 25 causes the dried agglomerates 26 to settle from the moist air 27 to the bottom of the separation chamber 25.
  • a fluid bed 28 conveys the dried agglomerates 20 through a chute 29 where they are fed to a fluidizer 30 (or some other device) and conveyed to a storage bin (not shown).
  • the moist air 27 is directed to a cyclone 31 where fins 32 are separated from the exit air 33. If desired, some other recovery device may be substituted for the cyclone.
  • the exit air 33 from the cyclone 31 may be conveyed to an intermittent bag filter (not shown) or other similar device for further recovery of fins, or alternatively, the exit air 33 may be discharged without further recovery of the fins.
  • the removal of the exit air 33 from the systems should be at such a rate so as to maintain the air pressure at the entrance to the drying chamber 21 at a pressure substantially the same as atmospheric pressure. If a large positive or negative pressure is maintained then expensive equipment may be necessary for the introduction of the agglomerates or larger fluctuation of temperatures may result.
  • FIGURE 4 illustrates details of the fluid bed 28 and is a section generally along the lines 4-4 of FIGURE 1.
  • the chute 29 is made up of a product conveying portion 35 and an air distributing portion 36 separated by a porous cloth 37. Dried agglomerates 20 are suspended on an air stream which passes from the air conveying portion 36 into the product conveying portion 35. This causes the agglomerated particles 26 to be held in suspension much in the manner of a fluid, and the fluidized particles flow downward in the chute 29 under the force of gravity. The action of the fluid bed cools a typical fiour product to about 70 to F. before it leaves the chute 29. Many variations of the construction of the fluid bed are readily apparent, for example, it is possible to have several fluid beds discharging in opposite directions from the separation chamber 25.
  • One method would be to have two fluid beds discharging in opposite directions meeting near the center of the separation chamber forming an inverted letter V.
  • Another possible embodiment would be to have the bottom of the separation chamber 25 shaped like the letter V having both fluid beds feeding to the center of the separation chamber and discharging through a single rotating air lock valve.
  • other conveying means such as a screw or bucket conveyor, for removal of the product from the separation chamber 25.
  • the drying chamber 21 should be as nearly vertical as possible. While drying certain types of agglomerates, the chamber may be tilted slightly, but preferably the chamber is vertical.
  • agglomerates which may be dried by the present method and apparatus include flour, starch, egg whites, milk, egg yolks, whole eggs, orange juice, coffee, tea, chocolate drink products, gelatin, pectin, inorganic salts, such as, ammonium sulfate, sodium hexametaphosphate, sodium chloride, silica gel, and gums, such as, guar gum, locust bean gum, gum tragacanth, and gum karaya.
  • inorganic salts such as, ammonium sulfate, sodium hexametaphosphate, sodium chloride, silica gel, and gums, such as, guar gum, locust bean gum, gum tragacanth, and gum karaya.
  • a method of drying fragile, moist flour agglomerates which comprises feeding said flour agglomerates into an air stream having a temperature of about 250 to about 400 F., co-currently passing the heated air and flour agglomerates downward through a drying zone wherein flour agglomerates and air move uninterrupted and vertically downward throughout the entire zone and wherein the velocity of movement of said flour agglomerates through the zone is influenced by gravity, feeding the air and flour agglomerates to a separation zone where the speed of the air stream is reduced thereby allowing the dried flour agglomerates to settle out of the air stream, cooling the dried flour agglomerates and then recovering the dried flour agglomerates from said separation zone.
  • a drying and separating apparatus which comprises a vertical tubular drying chamber, a gas heating means, means interconnecting said heating means and the top of said drying chamber for introducing heated gas and moist agglomerates into said drying chamber, said means for introducing including a receiving tube and a perforated, conical chamber interconnecting the top of said drying chamber and said receiving tube, a separation chamber connected to said drying chamber and having a cross-section greater than said drying chamber, means for removing gas from said separation chamber, and means for removing the dried agglomerates from said separation chamber.
  • a drying and separating apparatus which comprises an uninterrupted vertical tubular drying chamber; an air heater; means interconnecting said heater and the top of said drying chamber for introducing heated air and moist agglomerates into the drying chamber; said means for introducing including a receiving tube and a perforated, conical chamber interconnecting the top of said drying chamber and said receiving tube, a separation chamber having an inclined bottom member including porous material, an inlet for the air and moist agglomerates, and an outlet for air and associated with said drying chamber; means for passing gas upwardly through said porous material to fluidize particles contiguous with the bottom member; and means located at the lower end of the inclined bottom member for removing the fluidized particles.

Landscapes

  • Engineering & Computer Science (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mechanical Engineering (AREA)
  • General Engineering & Computer Science (AREA)
  • Microbiology (AREA)
  • Chemical & Material Sciences (AREA)
  • Food Science & Technology (AREA)
  • Polymers & Plastics (AREA)
  • Drying Of Solid Materials (AREA)
  • Dairy Products (AREA)
US270069A 1963-04-02 1963-04-02 Method and apparatus for drying agglomerates Expired - Lifetime US3262213A (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
US270069A US3262213A (en) 1963-04-02 1963-04-02 Method and apparatus for drying agglomerates
GB51428/63A GB1069838A (en) 1963-04-02 1963-12-31 Method and apparatus for drying agglomerates and the like
SE347/64A SE319140B (de) 1963-04-02 1964-01-13
CH29164A CH418980A (de) 1963-04-02 1964-01-13 Verfahren und Vorrichtung zum Trocknen von Agglomeraten

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
US270069A US3262213A (en) 1963-04-02 1963-04-02 Method and apparatus for drying agglomerates

Publications (1)

Publication Number Publication Date
US3262213A true US3262213A (en) 1966-07-26

Family

ID=23029765

Family Applications (1)

Application Number Title Priority Date Filing Date
US270069A Expired - Lifetime US3262213A (en) 1963-04-02 1963-04-02 Method and apparatus for drying agglomerates

Country Status (4)

Country Link
US (1) US3262213A (de)
CH (1) CH418980A (de)
GB (1) GB1069838A (de)
SE (1) SE319140B (de)

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3383774A (en) * 1965-12-23 1968-05-21 Gen Mills Inc Apparatus and method for treating pulverulent or granular material
US3514300A (en) * 1968-05-15 1970-05-26 Afico Sa Drying process
US4020564A (en) * 1975-09-17 1977-05-03 Nl Industries, Inc. Drier for temperature sensitive materials
US5683241A (en) * 1995-12-19 1997-11-04 Casselman; David S. Apparatus for heating bottle caps
US6240655B1 (en) * 1998-07-10 2001-06-05 Ball Semiconductor, Inc. Fluid exchange system and an associated spherical-shaped semiconductor integrated circuit manufacturing system
US9510617B2 (en) 2012-04-13 2016-12-06 Frito-Lay North America, Inc. Micropellets of fine particle nutrients and methods of incorporating same into snack food products
US10220558B2 (en) 2012-05-23 2019-03-05 Frito-Lay North America, Inc. Rotor assembly with one-piece finger member
US10914519B2 (en) * 2013-05-07 2021-02-09 Andritz Technology And Asset Management Gmbh Method for producing salts with a reduced water of crystallisation content

Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US205551A (en) * 1878-07-02 Improvement in grain steamer and drier
US493225A (en) * 1893-03-07 Henry b
US759527A (en) * 1902-11-01 1904-05-10 John Willard Irwin Grain drier and cooler.
US992295A (en) * 1909-01-11 1911-05-16 Fritz Tiemann Drying of non-pulverulent materials.
US1196979A (en) * 1914-06-11 1916-09-05 Oliver W Randolph Grain-drier.
US1428526A (en) * 1921-12-07 1922-09-12 Gen Rubber Co Process and apparatus for treating latex
GB275760A (en) * 1926-06-21 1927-08-18 Brynar James Owen An improved drying apparatus
US2240854A (en) * 1933-04-12 1941-05-06 Golden State Company Ltd Desiccating apparatus
US3010215A (en) * 1959-06-29 1961-11-28 Fuller Co Gas-solids heat exchanger

Patent Citations (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US205551A (en) * 1878-07-02 Improvement in grain steamer and drier
US493225A (en) * 1893-03-07 Henry b
US759527A (en) * 1902-11-01 1904-05-10 John Willard Irwin Grain drier and cooler.
US992295A (en) * 1909-01-11 1911-05-16 Fritz Tiemann Drying of non-pulverulent materials.
US1196979A (en) * 1914-06-11 1916-09-05 Oliver W Randolph Grain-drier.
US1428526A (en) * 1921-12-07 1922-09-12 Gen Rubber Co Process and apparatus for treating latex
GB275760A (en) * 1926-06-21 1927-08-18 Brynar James Owen An improved drying apparatus
US2240854A (en) * 1933-04-12 1941-05-06 Golden State Company Ltd Desiccating apparatus
US3010215A (en) * 1959-06-29 1961-11-28 Fuller Co Gas-solids heat exchanger

Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3383774A (en) * 1965-12-23 1968-05-21 Gen Mills Inc Apparatus and method for treating pulverulent or granular material
US3514300A (en) * 1968-05-15 1970-05-26 Afico Sa Drying process
US4020564A (en) * 1975-09-17 1977-05-03 Nl Industries, Inc. Drier for temperature sensitive materials
US5683241A (en) * 1995-12-19 1997-11-04 Casselman; David S. Apparatus for heating bottle caps
US6240655B1 (en) * 1998-07-10 2001-06-05 Ball Semiconductor, Inc. Fluid exchange system and an associated spherical-shaped semiconductor integrated circuit manufacturing system
US9510617B2 (en) 2012-04-13 2016-12-06 Frito-Lay North America, Inc. Micropellets of fine particle nutrients and methods of incorporating same into snack food products
US10220558B2 (en) 2012-05-23 2019-03-05 Frito-Lay North America, Inc. Rotor assembly with one-piece finger member
US10914519B2 (en) * 2013-05-07 2021-02-09 Andritz Technology And Asset Management Gmbh Method for producing salts with a reduced water of crystallisation content

Also Published As

Publication number Publication date
SE319140B (de) 1970-01-12
CH418980A (de) 1966-08-15
GB1069838A (en) 1967-05-24

Similar Documents

Publication Publication Date Title
US2893871A (en) Agglomeration process and apparatus
US2995773A (en) Process and apparatus for agglomerating pulverulent materials
US2054441A (en) Method and apparatus for drying liquid containing materials
US3615723A (en) Spray-drying apparatus
US2629938A (en) Method and apparatus for treating solids
US4073951A (en) Agglomeration method
US3262213A (en) Method and apparatus for drying agglomerates
US3186102A (en) Method of drying an insoluble particulate material
US3527647A (en) Agglomerating process and apparatus
US5042169A (en) Interstage separator
US3700461A (en) Gas suspersion agglomeration
US3795058A (en) Grid for fluidized bed apparatus
KR930006391B1 (ko) 열가소성 중합체를 구형 응집 입자로 전환시키는 방법
US3039107A (en) Agglomeration of spray-dried materials
US2312474A (en) Drying method
US5130156A (en) Method for agglomerating food powders
US3596699A (en) Apparatus for spray drying milk and the like
US3228115A (en) Apparatus for aggregating difficult to aggregate materials
JPH0638680A (ja) 乾燥粒子を湿潤、溶解させる装置および方法
US3549336A (en) Agglomerating pulverulent material by contacting with a film of jetted liquid
US3533805A (en) Method for the manufacture of low density products
US3068584A (en) Process for the treatment of divided materials
US4412978A (en) Method and apparatus for manufacturing improved puffed borax
US3313629A (en) Agglomerating process for powdered food solids or the like
US2728995A (en) Drying granular material