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Publication numberUS3925904 A
Publication typeGrant
Publication dateDec 16, 1975
Filing dateMay 14, 1974
Priority dateMay 14, 1974
Also published asCA1043097A1
Publication numberUS 3925904 A, US 3925904A, US-A-3925904, US3925904 A, US3925904A
InventorsKelly James G
Original AssigneeAmerican Brands
Export CitationBiBTeX, EndNote, RefMan
External Links: USPTO, USPTO Assignment, Espacenet
Method and apparatus for drying stillage
US 3925904 A
Stillage is flash dried in a drying conduit and chamber system by passing large volumes of air through the system having entrance temperatures in the range of about 325 DEG F to about 425 DEG F. Stillage material is rapidly circulated through the system a plurality of times. Water is separated from the stillage during each drying pass to form a dry (about 10% moisture content) nutrient food substance without emitting significant amounts of smoke or odors.
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Description  (OCR text may contain errors)

United States Patent [191 Kelly METHOD AND APPARATUS FOR DRYING STILLAGE [75] Inventor: James G. Kelly, Richmond, Va.

[73] Assignee: American Brands, Inc., New York,

22 Filed: May 14,1974

21 Appl. No.: 469,790

[52] US. Cl. 34/10; 34/57 A; 432/14 [51] Int. Cl. F26B 3/08 [58] Field of Search 34/10, 57 A; 432/14 [56] References Cited UNITED STATES PATENTS Christensen 34/10 X [451 Dec. 16, 1975 l/l946 Gordon 34/57 A 4/1974 l-ledstrom 34/l0 X Primary Examiner-John J. Camby Attorney, Agent, or Firm-Pennie & Edmonds ABSTRACT Stillage is flash dried in a drying conduit and chamber system by passing large volumes of air through the system having entrance temperatures in the range of about 325F to about 425F. Stillage material is rapidly circulated through the system a plurality of times. Water is separated from the Stillage during each drying pass to form a dry (about 10% moisture content) nutrient food substance without emitting significant amounts of smoke or odors.

6 Claims, 2 Drawing Figures METHOD AND APPARATUS FOR DRYING STILLAGE BACKGROUND OF THE INVENTION means, such as centrifuging or pressing. The liquid phase is further concentrated by evaporation providing a syrup including about 55% water. The solid materials or cake from the mechanical separation step and the syrup are mixed together to form a wet mixture which is then dried using dispersion or flash drying to reduce the moisture to about 10%.

In the past the flash drying processes that were used included limited air volumes, high drying chamber inlet air temperatures and material circulation techniques which often caused the emission of substantial amounts of smoke and odors during the drying operation.

The process and apparatus of the present invention is an improvement in the dispersion drying operation which uses substantially more air and lower temperatures to obtain a dried material which is improved in its nutrient value. The process is carried out with a'substantial reduction in smoke and odor and in fire and explosion hazards.

SUMMARY OF THE INVENTION Broadly, the present invention is an improvement in a stillage flash drying process in which cake, syrup and recycled stillage material having a moisture content of over about 10% is introduced into a large-volume rapidly moving air column heated to a temperature in the range of about 325F to about 425F, is mixed with the air, is carried a distance to a separator means where the particulate material is separated from the air and collected. Substantially all the material is then recycled a large number of times with the moisture content being reduced during each pass to dry the material until the moisture content is reduced to the desired level.

It is a'feature of the process that the product has improved nutritive value. It is also a feature that the process produces less smoke and odors.

BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a top plan view of the drying and FIG. 2 is an elevational view of apparatus that is used to practice the process of this invention.

DESCRIPTION OF THE PREFERRED EMBODIMENT Referring to FIGS. 1 and 2, air entering furnace 1 is heated and is caused to pass through the system in a generally counterclockwise path in which the air passes from furnace 1 through vertical mixing and drying column 2, through column extension duct 3, to Y- shaped duct section 4 where the air splits into two streams which flow along entrance ducts 6 and 7 to cyclone upper separator sections 8 and 9 of separator units 10. Two separator units are preferred but one, two or more may be used. The air passes around the cyclone entrance sections 8 and 9 causing the heavier stillage material to move to the outer peripheries of the separator sections 8' and 9 while the air is drawn off through the centered upper outlets 11 and 12 through cyclone exit conducts 13 and 14 and then down vertical air fan intake duct 16 through fan 17 and exhaust pipe 18. The exit temperature of the air is normally in the range of F to 200F.

Turning now to the flow pattern of the stillage material, wet material is fed into the system through down pipe 19 onto horizontal conveyor 21 where it is mixed with recycled stillage grain in a ratio from 5-40/1, then mixed further in subsequent conveyors 22 or mixers of appropriate length, orientation and capacity (not shown) and then fed by gravity, mechanical or pneumatic means (not shown) along feed chute 23 into the vertical column 2. Concentrated stillage syrup can be applied to the grain before or after the wet cake stillage is added to the recycled grain in whole or in part and at various points along the mixing conveyors or at a mixer immediately prior to introduction to the dryer column 2. The introduced material is mixed with and carried along by the heated gas stream until it is centrifugally separated in the separator portions 8 and 9 of the separator units 10. The separated and partially dried material then descends through cylindrical sections 26 and conical section 27 of the separator units 10 until the material reaches the bottom and is discharged through rotary locks 28. 5

During operation all the material is recirculated in the range of from 5-40 times with the composite mixture extracted at substantially the same rate off conveyor 21 as the rate of input of new material through pipe 19. Normally, drying down to about 10% is desired; however, it should be noted that each discrete portion of the material exiting pipe 31 is not exactly at 10% moisture but the average moisture content will be in the neighborhood of 10%. For example, if the system were operated with a 5,000 lbs./hr. input at 64% moisture and the material made only one pass about 54% of the moisture would have to be removed to bring the moisture down to 10%. However, if two passes were used in which the moisture reduction on the first pass was from 64% to 14% and from 14% to 6% on the second pass, about half the material would be extracted down to a 14% moisture content and one half down to a 6% moisture content thus providing the desired average of 10%. Again looking at averages, the average inlet moisture would drop to 39%. Thus, it is seen that as a larger number of passes is used, the average inlet moisture content is lowered. It should also be noted that with a greater volume of material in the system a large percent change in input flow through pipe 19 will have a lesser effect on the moisture content of the extracted mixture unless the large increase or decrease in input is continued for a substantial period of time.

The larger the number of recycle passes that are used the less water is extracted from each individual grain or particle during each drying pass. A plurality of passes, each interrupted by the time required to convey the material between passes, provides a retention time in the system adequate for proper moisture equilibration in each particle which is in part accomplished by moisture migration from the inside of the particles to their outside surface areas. The fact that the drying and evaporation can be more efficiently accomplished with lower temperatures and higher velocities of gas movement than previously employed is due in part to the use of step-by-step moisture extraction starting with re- 3 moval of moisture from the outside of the particle, migration of interior moisture to the surface and the subsequent removal of the migrated moisture. The system may, for example, have 25,000 to 200,000 lbs/hr. in circulation with an input and corresponding output of 5,000 lbs/hr.

Mixing of air and material is improved by drawing heated air up auxiliary duct 32 tangentially into ports 33 and 34 in the walls of column 2.

The introduction of tangential air increases turbulence, mixing and retention time of heavier particles. Though air is preferred as a drying medium process, superheated steam, other gases or mixture of gases can be used.

I claim:

1. A method of drying moist stillage material composed of moisture and moist particles having moisture pervaded throughout the particles comprising a. maintaining a rapidly moving gas stream emanating from a heat source and moving to one or more gas-stream and particulate-matter separator means which gas stream includes a columnar portion and is heated to a temperature sufficient to volatile moisture on and at the surface area of the particulate matter mixed therewith;

b. continuously introducing non-fluidized material into the columnar portion of the stream to cause the material to be mixed with it and heated by it;

c. causing the material to move a substantial distance along with the stream during which movement moisture on or at the surface area of the particulate matter is removed;

(1. separating the material from the gas stream;

e. collecting the separated material;

f. conveying and handling the collected material for a sufficient time to permit moisture in the interior of the particulate to migrate to the surface area;

g. introducing a substantial quantity of the treated material in non-fluidized form back into the columnar portion of gas stream after said moisture migration; and

h. repeating the above steps until the material has been substantially dried,

whereby the stillage is progressively and incrementally dried at temperatures that avoid any substantial reduction in the nutrient value of the stillage and without emitting significant amounts of smoke or odors.

2. The method of claim 1 in which the gas stream has a temperature of from about 425F to F.

3. The method of claim 1 in which the gas is air;

4. The method of claim 1 in which the gas is superheated steam.

5. The method of claim 1 in which the gas is a mixture of gases.

6. Apparatus for drying spent stillage comprising a. an elongated drying conduit;

b. gas pumping means for pumping a gas at high speed through the conduit;

c. non-fluidized stillage introducing means for introducing the non-fluidized stillage into the conduit as gas passes through the conduit;

(1. heating means for heating the gas prior to its entering the conduit;

6. separator means associated with the conduit for separating the material from the gas after it has travelled a distance in the conduit; and

f. recirculating means for introducing a substantial portion of the material back to the stillage introducing means while diverting a portion of the material to a separate location.

Patent Citations
Cited PatentFiling datePublication dateApplicantTitle
US2345238 *Jul 14, 1939Mar 28, 1944Chemical Foundation IncTreatment of distillery residues
US2393766 *Nov 28, 1942Jan 29, 1946Comb Eng Co IncDrying apparatus
US3808093 *Feb 15, 1972Apr 30, 1974Karlstad Mekaniska AbMethod and apparatus for drying pulp including heat exchange and temperature equalizing zones
Referenced by
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US7765368Jul 5, 2007Jul 27, 2010International Business Machines CorporationSystem, method and storage medium for providing a serialized memory interface with a bus repeater
EP0403608A1 *Nov 3, 1989Dec 27, 1990Akt Consultants Pty. LimitedApparatus and process for drying and comminuting matter
EP1955599A1 *Feb 9, 2007Aug 13, 2008Braunschweigische Maschinenbauanstalt AGMethod and device for drying by-products
WO2008095722A2Feb 8, 2008Aug 14, 2008Braunschweigische Maschb AnstaMethod and device for drying byproducts
U.S. Classification34/371, 432/14
International ClassificationF26B3/02, F26B3/10, F26B17/10, A23K3/00, F26B17/00
Cooperative ClassificationF26B3/10, F26B17/102, A23K3/005
European ClassificationF26B3/10, A23K3/00W, F26B17/10B2
Legal Events
Nov 26, 1986ASAssignment
Effective date: 19851219