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Publication numberUS3775863 A
Publication typeGrant
Publication date4 Dec 1973
Filing date20 Jul 1972
Priority date20 Jul 1972
Also published asDE2335577A1
Publication numberUS 3775863 A, US 3775863A, US-A-3775863, US3775863 A, US3775863A
InventorsUpdegrove L
Original AssigneeDay H Co
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Method and apparatus for drying particulate materials
US 3775863 A
Abstract
A method and apparatus for drying a particulate material such as resin pellets, fine chemicals, pigments, cosmetic powders and the like. The method involves mechanically agitating the material while sweeping it with pre-dried, heated air. The preferred form of apparatus includes a frustoconical tank having an agitator screw which is rotated upon its own axis to lift material and is simultaneously orbited around the wall of the tank. Air or other gas which has been heated and dried is introduced at the bottom of the tank and flows upwardly through the material. The air, carrying with it moisture released by the material, is discharged at the top of the mixer. The material can be mixed, granulated and dried in a single operation.
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United states Patent 1191 Updegrove METHOD AND APPARATUS FOR DRYING PARTICULATE MATERIALS [75] Inventor:

Ohio

[73] Assignee: The J. B. Day Company, Cincinnati,

Ohio

[22] Filed: July 20, 1972 [21] Appl. No.: 273,647

52 US. Cl ..34/166, 34/182, 259/40 58 Field of Search 34/166, 81, 182; 259/21, 40, 5

[56] References Cited 7 UNITED STATES PATENTS 2,668,764 2/1954 Nauta 259/40 2,345,063 3/[944 Nauta 259/40 3,618,070 10/1971 Loomans 25 9/40 Louis B. Updegrove, Terrace Park,

[ Dec. 4, 1973 Primary ExaminerCarroll B. Dority, Jr. Assistant Examiner-Larry l. Schwartz Attorney-James S. Hight et al.

[5 7 ABSTRACT A method and apparatus for drying a particulate material such as resin pellets, fine chemicals, pigments, cosmetic powders and the like. The method involves mechanicallyagitating the material while sweeping it with pre-dried, heated air. The preferred form of apparatus includes a frustoconical tank having an agitator screw which is rotated upon its own axis to lift material and is simultaneously orbited around the wall of the tank. Air or other gas which has been heated and dried is introduced at the bottom of the tank and flows upwardly through the material. The air, carrying with it moisture released by the material, is discharged at the top of the mixer. The material can be mixed, granulated and dried in a single operation.

14 Claims, 3 Drawing Figures PATENTEU DEC 4 I975 SHEET 10F 2 METHOD AND APPARATUS FOR DRYING PARTICULATE MATERIALS BACKGROUND OF THE INVENTION This invention relates to a method of, and apparatus for, drying materialsfsuch as textile resins, fine chemicals, pigments, pharmaceuticalsQpowdered metals and the like- In one important aspect, the invention is directed particularly to a method of drying materials to a very high degree of dryness, for example, to a final uum dryers have in the past proven to be the most ad-' vantageous. In "these dryers either bulk material is placed in a vessel or the material is placed on a carrier, such as a,tr ay, which is in turn placed in an oven or the like. A hard vacuum is drawn and heat is supplied from a heated surface such as the vessel walls.

While dryers ofthis type have gone into large scale commercial use, they are subject to several wellrecognized disadvantages. In the first place, vacuum equipment is inherently expensive to produce and expensive to operate and maintain. Moreover, it is extremely difficult at best and in most cases impossible to maintain close control of the product temperature in a vacuum dryer Another disadvantage is that vacuum dryers require a relatively long time to bring material down to a high degree of dryness. For example, commercial vacuum dryers at the present time require from 8 to 12 hours to reduce the moisture of Nylon 6 resin pellets from 2'percent to 0.01 percent moisture. Other less efficient types of commercial drying equipment require as ns a 3. ho r $93299PIRUHQIXEQEL eration. a v

.The present invention is directed in partto a method of drying materials to a high degree of dryness in a-substantially shorter period of time than has heretofore been possible. For example, the present method is effective to dry Nylon 6 resin pellets from 2 percent to (1. 01 percent moistgre content in 4 hours, which represents a time saving of from 50 percent to 66 percent as compared to the best vacuum dryers, and a time saving of some 89 percent compared to other forms of commercial drying equipment.

-It is a further object of the present invention to provide a drying method which can be carried out in apparatus costing substantially less than vacuum drying ap- The present drying method makes effective use of two driving forces. The first force is heat transferred from the air to the product whichcauses water vapor' I vapor pressure as compared to the vapor pressure of paratus. Moreover, the apparatus required to practice the present invention is not only less expensive to install, but also costs substantially less to operate and maintain.

More particularly, the present invention is predicated in part upon the concept of drying material by the combined action of mechanically agitating the material while sweeping it with a stream of hot pre-dried air or other gas. The material is preferably agitated so that it flows both transversely of the airstream and in counter-.

current relation to it.

the moisture in the material being dried.

When treating material in accordance with the present method, particularly in the preferred form of apparatus described below, optimum use is made of both of these driving forces. In the first place, the mechanical agitation of the material results in'the airstream being continuously exposed to different material as the air passes from the inlet to the outlet. Thus, an optimum heat transfer is effected between the air and the materiaL'All of the material being processed is kept at a uniform controlled temperature with no localized hot spots. r r

As a result, the heat in the air is effectively utilized in vaporizing moisture, from the product. This vaporization in turn rapidly lowers the temperature of the air. We have empirically determined that this combined action enables the use of air at a substantially higher temperature than would otherwise be possible without causing product deterioration. For example, if a product deteriorates in some manner, e.g., discolors, melts, reacts' or the like, at a temperature of F., I have determined that air temperature in the present method need not be limited to 120 F., but may be substantially higher, for example, as high as 270 F. The use of this higher temperature air accelerates vaporization and materially shortens the drying time. It will be appreciated that if the material is oxygen sensitive, other gases, such as carbon dioxide or nitrogen, can be used in place of air.

It is another aspect of the present invention to provide a method in which material can be effectively dried, granulated and mixed in a single operation. This aspect of the present invention is-useful not only in drying'material to a high degree of dryness, but also in drying'material to a more moderate degree of dryness, for

example, to a moisture content of from 0.1 percent to inner wall of the tank. At the same time, the agitator revolves on its own axis in such a manner as to'lift the material from the bottom toward the top of the tank.

In accordance with the present invention, the tank is further provided with a porous air inlet connection adjacent to the lower portion of the tank wall. Air is supplied to this inlet from a system including a pump, or compressor, which forces air through a dryer and a heater. The air which is pre-dried to a low relative humidity enters the vessel at a temperature of from ambient temperature to 400 F. and at'a pressure less than 25 psi. The air is preferably heated to a temperature close to the temperature at which it would heat the product to a point which would cause product deterioration. The air pressure is sufflciently high to force the air upwardly through the material at a flow rate below the flow rate at which the material would spout.

As the agitator moves through the material, it intermixes and granulates the material and continuously injects fresh material into the airstream. The mixer not only shifts the material in a transverse or horizontal plane, but also causes vertical displacement of the material, the material being carried upwardly by the screw and then flowing downwardly, countercurrent to the airstream. The hot, dry air transfers heat to the material in the tank, causing rapid evaporation which lowers the air temperature so that the air which has passed completely through the material and is discharged is moisture laden, relatively cool air at a temperature not substantially above the product temperature. For example, during a part of a typical operation, air is introduced at 270 F. and exits at 100 F. with product temperature being 97 F. and being substantially uniform throughout the tank. As will be appreciated, both air exit temperature and product temperature increase during the drying cycle.

One of the principal advantages of the present apparatus is that optimum heat and moisture transfer is effected between the airstream and material. The entering airstream is continuously brought into contact with fresh product so that no hot spot is developed. Moreover, the airstream passes through a relatively long path of product so it has ample contact to give up heat and pick up moisture. This again contributes to the overall efficiency of the operation resulting in the substantially decreased drying time required.

A further advantage of the present apparatus is that it is substantially less expensive than vacuum drying equipment not only from the point of view of initial investment, but is also much less expensive to operate and maintain.

Another advantage of the present apparatus is that it facilitates'drying and granulation and mixing in a single operation.

A still further advantage of the present apparatus is that it can be utilized to dry materials which are originally in a paste condition or in which the particles are originally moist and sticky.

These and other objects and advantages of the present invention will be more readily apparent from the 3. As shown in FIG. 1, mixer comprises a vessel, or

, tank, 12 of generally inverted frustoconical configuraball and socket joint or the like, for supporting the following detailed description of the drawings illustrating a preferred embodiment of the invention.

DESCRIPTION OF THE DRAWINGS DESCRIPTION OF THE APPARATUS A preferred form of mixer 10 embodying the present invention is shown in FIG. 1 and a drying system 11 utilizing such a mixer is shown in schematic form in FIG.

lower end of a helical agitator screw 16. Joint 15 is located on the vertical center line of the vessel. Agitator screw 16 includes a thin, helical plate 17 which is carried by an elongated shaft 18.

The lower end of shaft 18 is carried by joint 15, while the upper end of the shaft is joumalled in a suitable bearing carried by the outer end of radial support arm 20. The inner end of support arm 20 is rotatably supported as at 21 in the center of a cover member 22. A drive 23 is interconnected with arm 20 and shaft 18. This drive is effective to cause the arm 20 to revolve in a plane perpendicular to the axis of the tank at a relatively low speed, for example, two revolutions per minute. Drive 23 is also effective to rotate shaft 18 about its own axis, at a substantially higher speed, for example, a speed of 64 revolutions per minute.

It is to be understood that the mechanical details of the drive for arm 20 and screw 18 constitute no part of the present invention. Such mechanical drives are well known in the art. Moreover, while the drive is shown as including only a single motor 24 which is effective, through suitable gearing, to drive both radial arm 20 and agitator screw 16, it is to be understood that if desired separate motors can be provided for driving the arm and screw.

Shaft 18 is mounted so that it intersects the vertical center line of tank 10 at an angle equal to half of the vertical angle of the cone defined by the walls of tank 12. In operation, the support arm 20 revolves in a horizontal plane and causes the shaft 18 to orbit, or generate a conical shape, so that the agitator screw moves around the inside surface of wall 12 and deflects material away from the wall toward the center of the tank. At the same time, the agitator screw is revolved about its own axis, i.e., the axis of shaft 18 so that material within the tank is carried upwardly by the screw from the bottom toward the top of the'tank.

In addition to the elements described above, mixer 10 includes a material discharge port adjacent to the lower end of the tank. This discharge port may be connected to a discharge chute, such as chute l9, and the port may be opened or closed by a suitable valve, such as a sliding gate valve, rotating plug valve, or the like, the valve being operated by an actuator such as handle 25. Additionally, the cover 22 is provided with openings (not shown) for introducing material into the mixer and with a suitable air discharge filter 26 (shown in FIG. 3, but not shown in FIG. 1). This filter, which discharges moisture-laden air from the mixer, can either be vented to atmosphere directly or through an air conduit if desired. It will be understood that if a gas, such as nitrogen, is employed, it can be recycled through the heater and dryer if desired.

In accordance with the present invention, a lower portiom of the wall of tank 12 is provided with an air inlet port 27. This port is covered with a porous plate 28 or other member for defusing the air stream entering the mixer to prevent high pressure localized air jets which would cause the material to spout. One suitable form of plate is a sintered stainless steel plate. Such plates are manufactured by Pall-Trinity Micro Corporation and are designated porous type PSS plates Grades D and E. The sizes of the holes in these plates are 35 microns and 65 microns, respectively. The area surrounding air port 27 and plate 28 is enclosed by the walls of a duct-forming chamber 29. This chamber is connected to an air inlet conduit 30.

A complete drying system incorporatingmixer is dryers form no part of the present invention and since the construction is well known, it is considered unnecessary to describe the details of the dryer with particularity.

The inlet of dryer 32 is interconnected to compressor 31 by air conduit 33. The dryer is also interconnected through conduit 35 and valve 36 to a heater 34. Again, heater 34 can be of any conventional type such as. an

electrical air heater, gas heater, steam heater or the like. The outlet of heater 34 is connected to air inlet conduit of the mixer. I v

This dryer system finds particular utility in the drying of materials in an ultra high degree of dryness; The term ultra high degree of dryness as used herein refers to materials dried to'a very low moisture content of from, for example, 0.0] percent to 0.05 percent moisture. An example of such materials would be textile resin pelletssuch as Nylon pellets. Pellets of other resins, such as Dacron and polyester polymers, also fall in this category. v

in drying Nylon pellets or other material to an ultra high condition the material is, introduced into the mixer 10. Drive 23 causes radialarm 20.to revolve slowly and causes agitator screw to rotate about its own axisat a higher speed. Thus the material is subjected to three distinct actions. In the'first place, the screw agitator rotating on the axis of the shaft 18 lifts material from the bottom towardthe top of the tank. Simultaneously, the agitator orbits around the wall of the tank as the upper end of the agitator is carried by radial arm 20. This action tends to move material away from the wall of the tank deflecting it toward the center. in the third place, the material lifting upwardly by the screw gravitates downwardly intermixing with the material which is spiraled upwardly. I

- At the same time, the air supply provided by compressor or blower 31 is dried by dryer 32 to a very dry condition for example to a dew point of from 1 0F. to 40F., a preferred dryness being a dew point of 40F. Air flows from the dryer to heater 34 where the tem- 'perature of the air is elevated to a temperature below that at which the air would raise the product temperature to a point causing deterioration of the material being processed. Depending upon this material the temperature-may be frorn room temperatureto approximately 400F. For Nylon a preferred temperature is of the order of 200F. In any event, this air temperature can-be substantially above the critical maximum temperature for the material. Thus, we have determined empirically that if a material deteriorates at a temperature of 150F. for example, the air temperature may be approximately 300F.

This hot, dry air is introduced through chamber 29 and porous plate 28 into the bottom of the tank 12. The air is preferably fed to the tank at a rate of from approximately one cubic foot of air per cubic foot of material to approximately 13 cubic feet of air per cubic foot of material per minute. The pressure of air in chamber 29 is relatively low, e.g., less than 25 psi, and is preferably less than 10 psi. The optimum pressure will vary with the size, density, etc., of the material being dried. in each case,.however, the air pressure is idized bed in the material and may be from one to two magnitudes less than the pressure which would create such a bed.

As the hot dry air enters the tank, it is continuously brought into contact with different material. The hot air. heats the materialand causes evaporation of the water from the material. This evaporation in turn causes the air temperature to be lowered. As the air moves upwardly, it gives up heat and picks up moisture as it passes through an elongated conical column" of material which is being thoroughly agitated. As a result, the air causes the temperature of the material to be raised in a very uniform fashion, i.e., there are not hot and cold spots,'and no more thah a nominal difference in temperature between different portions of the material. When the air reaches the top of the level of material, the air has given up much of its heat and has absorbed a considerable amount of moisture. For exam ple, the air in the illustration given, exits through filter 25at a temperature of approximately 100 F.

It is extremely important to the'present process that the air is constantly being brought into contact with different portions of material so that the air' temperature is effectively utilized in vaporizing moisture without locally heating the material being dried to a temperature which would result in deterioration of the product. In other words, the highly effective mixing action and air path provided in mixer 10 enables the use of air at a much higher temperature than the temperature at which the material deteriorates. As a resultof the effective drying action provided by the present system, the

ple,. in approximately 4 hours as opposed to the 8-12 hours required utilizing the best prior art vacuum equipment, 563 36 hours utilizing other ty pes of commercial equipment.

- In addition to its utility in drying materials to an ultra high degree of dryness, the present equipment is also advantageous for use in drying materials to a somewhat higher moisture'content, e.g., from 0.5 percent to 2 percent. One of the principal advantages of the present systern in drying these materials (which advantage is also obtained when-drying materials to an ultra dry condition) is that three operations are performed on the material simultaneously. Specifically, the materials are mixed, granulated and dried simultaneously in one operation within the mixer. 10.Materials which can be treated in this manner. include fine chemicals, pigments and dye stuffs, cosmetic powders, various resins and the like.

In treating these materials, the materials are introduced into the tank 12 and the drive 23 started to cause support arm 20 to revolve and to rotate agitator screw 16 upon its own axis. Simultaneously, air at a temperature from room temperature to 400 F. and with a dew point of from lO F. to 40 F. is introduced into the bottom of the tank through porous plate 28. Again, the air pressure is high enough to force air through the material, but is less than that which would cause spouting of the material. The air temperature is less than the temperature which would elevate the material temperature high enough to cause deterioration of the prod.-

uct.

The degree of the dryness of the air supplied is dependent in part upon the ultimate dryness required of the product and in part upon the economics of the process. For material which is to be dried to a lesser degree of dryness, e.g., 0.5 percent air at -l F. dew point can be employed. On the other hand, for some materi als which are to be dried to a high degree of dryness, or which are inherently difficult to dry, it may be desirable to utilize air at 40 F. dew point. While air having a dew point below 40 F. could be used, it is not usually economically attractive using presently available equipment. As the air and materials are intermixed in the tank, the solid materials are mixed and granulated. At the same time, the hot, dry air which is constantly being brought into contact with different portions of the material effects an optimum heat transfer of the material to cause the moisture in the material to be vaporized and carried off by the swept air. The air and entrained moisture are discharged through filter 26.

From the above disclosure of the general principles of the present invention and the above description of. a preferred embodiment, those skilled in the art will readily comprehend various modifications to which the invention is susceptible. Thus, for example, the present method can be carried out utilizing different apparatus from the preferred form of apparatus shown. By way of example, such apparatus can include a tank having a conical bottom and cylindrical side walls of the type shown in Nauta US. Pat. No. 2,345,063. Alternatively, the mixer can include an agitator screw of conical configuration or can include twin agitators. Also, the upper end of the agitator screw can be shifted in a horizontal plane with a compound motion including a radial component as shown in Fox U.S. Pat. No. 3,338,562. Therefore, I desire to be limited only by the scope of the following claims.

Having described my invention, I claim:

1. A method of simultaneously mixing granulating and drying material, comprising the steps of:

placing said material in a vessel having conical walls sloping inwardly toward a bottom wall,

agitating said material by means of a screw agitator rotating upon its own axis and having its axis moved within the container, whereby said material is elevated and moved away from the container wall,

and simultaneously introducing into the lower portion of said container pre-dried, heated air at a flow rate less than the flow rate required to cause spouting of said material.

2. The method of claim 1 in which the air temperature is less than that required to raise the material to a temperature at which the material would degrade.

3. The method of claim 2 in which the air temperature is above the temperature at which the material would degrade.

4. The method of claim 1 in which the agitation is effective to maintain the entire quantity of material at a substantially uniform temperature.

5. The method of claim 4 in which the material is heated to a final temperature and the air emerges from contact with the material at a temperature not appreciably above the final material temperature.

6. The method of claim 1 in which air is swept over said material at a rate of from one to 13 cubic feet of air per cubic foot of material per minute.

7. A device for simultaneously granulating and drying material comprising:

a mixing vessel having a frustoconical side wall taper ing inwardly toward a bottom wall,

an agitator screw,

means rotatably supporting the lower end of said agitator screw adjacent to the bottom wall,

a support arm disposed in the upper portion of the vessel,

means shifting said support arm in a plane transverse to the axis of the vessel, said support arm carrying the upper end of said agitator screw,

means for rotating said screw about its own axis,

means for introducing pre-dried, heated air under relatively low pressure to the lower portion of said vessel,

and means for discharging air from the upper portion of said vessel.

8. The apparatus of claim 7 in which the means for introducing air comprises a porous plate.

9. The apparatus of claim 7 in which said porous plate is disposed closely adjacent to the bottom wall of said mixer.

10. A system for drying materials, said system comprising: I

a mixing vessel having a frustoconical side wall tapering inwardly toward a bottom wall,

an agitator screw,

means rotatably supporting the lower end of said agitator screw adjacent to the bottom wall,

a support arm disposed in the upper portion of the vessel,

means shifting said support arm in a plane transverse to the axis of the vessel, said support arm carrying the upper end of said agitator screw,

means for rotating said screw about its own axis,

an air inlet disposed adjacent to the lower portion of said vessel,

means for discharging air from the upper portion of said vessel,

an air dryer,

means for supplying air under pressure to said air dryer,

an air heater interconnected to said air dryer for heating said air,

and conduit means interconnecting said air heater and said air inlet.

11. The system of claim 10 in which said air inlet includes a porous plate.

sel.

14. The system of claim 10 in which air is supplied to the vessel at a rate of from one cubic foot of air to 13 cubic feet of air per cubic foot of material in the vessel per minute.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
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US2668764 *3 Oct 19509 Feb 1954Nauta Johannes EMethod and device for conching a chocolate mass and the like
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Referenced by
Citing PatentFiling datePublication dateApplicantTitle
US3913238 *26 Jul 197321 Oct 1975Day J H CoMethod and apparatus for drying particulate materials
US4101116 *27 Sep 197618 Jul 1978Motan Gesellschaft Mit Beschrankter HaftungApparatus for mixing granulated and/or pulverous materials
US4127333 *31 Mar 197728 Nov 1978Instytut Chemii PrzemslowejContinuously operated cone-and-screw mixer
US4159580 *25 Nov 19773 Jul 1979Welch Jr RichardGrain drying bin
US4534658 *29 May 198413 Aug 1985Isem B.V.Mixing apparatus, having seals which may be satisfactorily cleaned, particularly for the pharmaceutical industry
US4588301 *30 Sep 198313 May 1986Alfred BolzConical screw mixer
US4668099 *16 Sep 198526 May 1987Alfred BolzConical spiral mixer with spherical sealing body in the bottom opening
US4734149 *20 Mar 198729 Mar 1988Warner-Lambert CompanyApparatus for heatsealing gelatin capsules containing a medicament
US4915506 *18 Aug 198810 Apr 1990Hosokawa Micron Europe B.V.Apparatus for drying material which is mixed with a solvent
US4980029 *23 Jan 198925 Dec 1990Alfred Bolz Gmbh & Co. KgApparatus for treating waste materials
US5123748 *27 Jun 199023 Jun 1992N.V. Machinefabriek TerletMixing device with central thermal element
US5255444 *4 Feb 199226 Oct 1993Krauss-Maffei AktiengesellschaftMicrowave drying/mixing apparatus
US5649765 *7 May 199622 Jul 1997Littleford Day, Inc.Conical mixer apparatus with contamination-preventing orbit arm assembly
US5709036 *3 May 199620 Jan 1998Haleen; Len W.Aggressive convective drying in a conical screw type mixer/dryer
US6065223 *23 Aug 199323 May 2000Gode; GaborDevice utilizing solar energy, especially for drying and roasting of agricultural-, as well as food processing products, finalizing distillation and evaporation, separating of complicated compounds
US738742720 Oct 200617 Jun 2008Bristol-Myers Squibb CompanyMethod for blending heat-sensitive material using a conical screw blender with gas injection
US7908765 *22 Dec 200622 Mar 2011Collette NvContinuous granulating and drying apparatus
US20080094934 *20 Oct 200624 Apr 2008Win-Chin ChiangConical screw blender
US20080095752 *20 Oct 200624 Apr 2008Win-Chin ChiangMethod for extending the shelf-life of powdered nutritional formulations which contain viable probiotics
CN103759512A *7 Jan 201430 Apr 2014合肥杰事杰新材料股份有限公司Blast drier
CN105004156A *23 Jul 201528 Oct 2015合肥维巧食品科技有限公司Camellia drying device
DE4103455A1 *6 Feb 199113 Aug 1992Krauss Maffei AgMischertrockner
EP1068802A2 *14 Jul 200017 Jan 2001Emmerich TetkovApparatus and process for drying of heat-sensible material
EP1068802A3 *14 Jul 20001 Oct 2003Emmerich TetkovApparatus and process for drying of heat-sensible material
Classifications
U.S. Classification34/166, 366/144, 366/287, 366/192, 34/182
International ClassificationB01F13/02, F26B11/12, B01F15/06, B01F7/00, F26B11/00, F26B17/00, B01F7/16, B01F7/30, B01F15/00, B01F13/00
Cooperative ClassificationB01F13/0211, B01F7/302, B01F7/00991, B01F7/00416, F26B11/12, B01F15/063
European ClassificationB01F7/30B, B01F13/02C, F26B11/12, B01F15/06C
Legal Events
DateCodeEventDescription
29 Jun 1987AS01Change of name
Owner name: DAY MIXING COMPANY
Owner name: LFB INC.
Effective date: 19810629
29 Jun 1987ASAssignment
Owner name: DAY MIXING COMPANY
Free format text: CHANGE OF NAME;ASSIGNOR:LFB INC.;REEL/FRAME:004733/0498
Effective date: 19810629
Owner name: J.H. DAY COMPANY
Free format text: CHANGE OF NAME;ASSIGNOR:DAY MIXING COMPANY;REEL/FRAME:004733/0496
Effective date: 19861230
2 Nov 1981ASAssignment
Owner name: LFB INC., 4932 BEECH STREET, CINCINNATI, OH 4521
Free format text: ASSIGNMENT OF ASSIGNORS INTEREST.;ASSIGNOR:LEBLOND INCORPORATED;REEL/FRAME:003934/0446
Effective date: 19810627
2 Nov 1981AS02Assignment of assignor's interest
Owner name: LEBLOND INCORPORATED
Effective date: 19810627
Owner name: LFB INC., 4932 BEECH STREET, CINCINNATI, OH 45212